Title of Invention	A CONTINUOUS PROCESS FOR PRODUCING POLYMIDES FROM AMINONITRILES
Abstract	The continuous method for producing a polyamide by reacting at least one aminonitrile with water, comprising the following steps: (1) reaction of at least one aminonitrile with water at a temperature of between 90 and 400°C and a pressure of between 0.1 and 15 x 10<Sup>6</Sup> Pa in a tubular flow reactor containing packing material of a Bronsted acid catalyst selected from beta zeolite, sheet silicate or titanium dioxide packing materials, as well as metallic packing materials, which yields a reaction mixture; (2) further reaction of the reaction mixture at a temperature of between 150 and 400 °C and a pressure which is lower than the pressure in step 1, where the temperature and pressure are selected such that a first gaseous phase and a first liquid or a first solid phase or a mixture of a first solid and a first liquid phase is obtained, and the first gaseous phase is separated from the first liquid or first solid phase or the mixture of the first liquid and first solid phase; and (3) addition of the first liquid or first solid phase or the mixture of first liquid and first solid phase to a gaseous or liquid phase containing water, at a temperature of between 150 and 370°C and a pressure of between 0.1 and 30 x 10<Sup>6</Sup> Pa, resulting in a product mixture.

Title of Invention

A CONTINUOUS PROCESS FOR PRODUCING POLYMIDES FROM AMINONITRILES

Abstract

The continuous method for producing a polyamide by reacting at least one aminonitrile with water, comprising the following steps: (1) reaction of at least one aminonitrile with water at a temperature of between 90 and 400°C and a pressure of between 0.1 and 15 x 10<Sup>6</Sup> Pa in a tubular flow reactor containing packing material of a Bronsted acid catalyst selected from beta zeolite, sheet silicate or titanium dioxide packing materials, as well as metallic packing materials, which yields a reaction mixture; (2) further reaction of the reaction mixture at a temperature of between 150 and 400 °C and a pressure which is lower than the pressure in step 1, where the temperature and pressure are selected such that a first gaseous phase and a first liquid or a first solid phase or a mixture of a first solid and a first liquid phase is obtained, and the first gaseous phase is separated from the first liquid or first solid phase or the mixture of the first liquid and first solid phase; and (3) addition of the first liquid or first solid phase or the mixture of first liquid and first solid phase to a gaseous or liquid phase containing water, at a temperature of between 150 and 370°C and a pressure of between 0.1 and 30 x 10<Sup>6</Sup> Pa, resulting in a product mixture.

Full Text	Continuous process for producing polyamides from aminonitriles The present invention relates to a continuous process for producing polyamides from aminonitriles and water at elevated temperature and elevated pressure. US 4,629,776 describes a catalytic process for producing polyamides from w-aminonitriles such as w-amino-capronitrile (ACN). ACN is reacted with water in the presence of a catalytic amount of an oxidized sulfur compound as catalyst. Sulfuric acid is an example of the catalyst used. US 4,568,736 describes a similar catalytic process for producing polyamides. The catalyst used in this case is an oxygen-containing phosphorus compound, phosphoric acid or a phosphonic acid. Complete removal of catalyst is virtually impossible in either process. The presence of catalyst in the polymer can hinder the building of high molecular weight polymers and compromise later processing operations, for example spinning. Moreover, the level of volatiles in the polymers obtained is high, so that the polyamides are difficult to process. EP-A-0 479 306 describes the production of polyamides from w-arnjnonitriles. The w-aminonitriles are reacted with water in the presence of an oxygen-containing phosphorus compound as catalyst. Once a reaction temperature from 200 to 260°C has been obtained, ammonia and water are continuously removed by decompressing and at the same time water is continuously added, the pressure being selected within the range from 14 to 24 x 106Pa (14-24 bar). DE-A-43 39 648 relates to a process for producing caprolactam by reacting aminocarbonitriles with water in the liquid phase using heterogeneous catalysts. Suitable heterogeneous catalysts include acidic, basic or amphoteric oxides of the elements of main groups 2, 3 and 4 of the Periodic Table. Titanium dioxide can be used, for example. The catalyst is used in the form of extrudates, for example. A continuous reaction requires intensive transverse mixing within the tubular reactors used, to even out concentration and temperature gradients. In addition, any axial backmixing should be as low as possible. Only effective suppression of axial backmixing, or axial dispersion, makes it possible to achieve a plug flow profile which guarantees a narrow residence time distribution and a defined equal residence time for all volume elements in the tubular reactor. It is an object of the present invention to provide a continuous process for producing polyamides from aminonitriles using a tubular reactor which substan¬tially prevents backmixing and provides a narrow residence time distribution. In addition, improved reaction conditions, a lower temperature and lower pressure shall be obtainable. We have found that this object is achieved according to the invention by a continuous process for producing a polyamide by reacting at least one aminonitrile with water, comprising the following steps: (1) reacting at least one aminonitrile with water at a temperature from(90 to 400°C and a pressure from 0.1 to 15 x 106 Pa in a flow tube containing packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements and metallic packing elements to obtain a reaction mixture, (2) further reacting the reaction mixture at from 150 to 400°C and a pressure which is lower than the pressure in step 1, the temperature and pressure ) being selected so as to obtain a first gas phase and a first liquid or a first ; -." solid phase or a mixture of first solid and first liquid phase, and the first gas \ phase is separated from the first liquid or first solid phase or the mixture of first liquid and first solid phase, and (3) admixing the first liquid or the first solid phase or the mixture of first liquid and first solid phase with a gaseous or liquid phase comprising water at a temperature from 150 to 370°C and a pressure from 0.1 to 30 x 106 Pa to obtain a product mixture. The present invention further provides a continuous process for producing a polyamide by reacting at least one aminonitrile with water, comprising the following steps: (1) reacting at least one aminonitrile with water at a temperature from(l90 to } 400°C and a pressure from 0.1 to 15 x 106 Pa in a flow tube containing packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements and metallic packing elements to obtain a reaction mixture, (2) * further reacting the reaction mixture at from 150 to 400°C and a pressure which is lower than the pressure in step 1, the temperature and pressure being selected so as to obtain a first gas phase and a first liquid or a first solid phase or a mixture of first solid and first liquid phase, and the first gas phase is separated from the first liquid or first solid phase or the mixture of first liquid and first solid phase, and (3) admixing the first liquid or the first solid phase or the mixture of first liquid and first solid phase with a gaseous or liquid phase comprising water at a temperature from 150 to 370°C and a pressure from 0.1 to 30 x 106 Pa in a flow tube containing packing elements of a Bronsted acid catalyst selected, from beta-zeolite, sheet-silicate or titanium dioxide packing elements and metallic packings to obtain a product mixture. The foregoing processes preferably further comprise the following step: (4) postcondensing the first liquid or the first solid phase or the mixture of first liquid and first solid phase at a temperature from 200 to 350°C and a pressure which is lower than the pressure in step 3, the temperature and pressure being selected so as to obtain a second, water- and ammonia- comprising gas phase and a second liquid or second solid phase or a mixture of second liquid and second solid phase, which each comprise the polyamide. The present invention further provides a continuous process for producing a polyamide by reacting at least one aminonitrile with water, comprising the following steps: (1) reacting at least one aminonitrile with water at a temperature from 90 to 300°C and a pressure from 0.1 to 15 x 106 Pa in a flow tube containing packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements and metallic packing elements to obtain a reaction mixture, (2) further reacting the reaction mixture at from 150 to 400°C and a pressure which is lower than the pressure in step 1, the temperature and pressure being selected so as to obtain a first gas phase and a first liquid or a first I solid phase or a mixture of first solid and first liquid phase, and the first gas phase is separated from the first liquid or first solid phase or the mixture of first liquid and first solid phase, and " (4) postcondensing the first liquid or the first solid phase or the mixture of first liquid and first solid phase at a temperature from 200 to 350°C and a pressure which is lower than the pressure in step 3, the temperature and pressure being selected so as to obtain a second, water- and ammonia-comprising gas phase and a second liquid or second solid phase or a mixture of second liquid and second solid phase, which each comprise the polyamide. The inventors have found that the use of a combination of titanium dioxide packing elements and metallic packing elements in flow tubes (also known as tubular ■ reactors) leads to a narrow residence time distribution of the reaction mixture in the tube. In addition it is possible to lower the reaction temperature required for converting the reaction mixture and the reaction pressure in the flow tubes. The " " . i process of the invention thus leads to an improvement in product homogeneity and ; product quality while at the same time reducing the energy input into the reaction , mixture. The principle of the process of the invention is described in prior DE-A-197 09 390, unpublished at the priority date of the present invention. An aminonitrile is reacted with water in the flow tube in a first step, subjected to a partial hydro lytic polymerization and further processed in subsequent reaction steps. The overall process comprises 3 or 4 steps. The flow tubes equipped according to the invention can be used in steps (1) and (3). The aminonitrile in the mixture can be in principle any aminonitrile, i.e., any \ compound having both at least one amino group and at least one nitrile group, (w-) Aminonitriles are preferred, especially co-aminoalkyl nitriles having from 4 to 12 5 carbon atoms, more preferably 4 to 9 carbon atoms, in the alkylene moiety, or an aminoalkylaryl nitrile having from 8 to 13 carbon atoms, preferred aminoalkylaryl nitriles being aminoalkylaryl nitriles which have an alkylene group of at least one carbon atom between the aromatic unit and the amino and nitrile group. Especially preferred aminoalkylaryl nitriles are those which have the amino group and nitrile ; ) group in the 1,4 position relative to each other. The co-aminoalkyl nitrile used is preferably a linear co-aminoalkyl nitrile in which the alkylene moiety (-CH2-) preferably contains from 4 to 12 carbon atoms, more preferably from 4 to 9 carbon atoms, such as 6-amino-l-cyanopentane (6- \| aminocapronitrile), 7-amino-l-cyanohexane, 8-amino-l-cyanoheptane, 9-amino-l- ! cyanooctane, 10-amino-1 -cyanononane, particularly preferably 6-aminocapronitrile. j 6-Aminocapronitrile is customarily obtained by hydrogenation of adiponitrile according to known methods, described for example in DE-A 836,938, DE-A 848,654 or US 5,151,543. Of course, it is also possible to use mixtures of a plurality of aminonitriles or mixtures of an aminonitrile with further comonomers, such as caprolactam or the below-defined mixture. In a particular embodiment, especially if copolyamides or branched or chain-lengthened polyamides are to be prepared, the following mixture is used instead of pure 6-aminocapronitrile: from 50 to 99.99, preferably from 80 to 90, % by weight of 6-aminocapronitrile, from 0.01 to 50, preferably from 1 to 30, % by weight of at least one dicarboxylic acid selected from the group consisting of aliphatic C4-C10-a,co-dicarboxylic acids, aromatic C5-C12-dicarboxylic acids and C5-C5-cycloalkanedicarboxylic acids, from 0 to 50, preferably from 0.1 to 30, % by weight of an a,co-diamine having from 4 to 10 carbon atoms, from 0 to 50, preferably from 0 to 30, % by weight of an a,co-C2-Ci2-dinitrile, and from 0 to 50, preferably from 0 to 30, % by weight of an a,co-C5-Ci2-amino acid or of the corresponding lactam, from 0 to 10% by weight of at least one inorganic acid or salt thereof, the individual weight percentages adding up to 100%. Suitable dicarboxylic acids include aliphatic C4-C10-ct,-dicarboxylic acids such as succinic acid, glutaric acid, adipic acid, pimelic acid, suberic acid, azelaic acid, sebacic acid, preferably adipic acid and sebacic acid, particularly preferably adipic acid, and aromatic Cs-Ci2-dicarboxylic acids such as terephthalic acid and also C5-C8-cycloalkanedicarboxylic acids such as cyclo-hexanedicarboxylic acid. Suitable a,co-diamines having from 4 to 10 carbon atoms include tetramethylene-diamine, pentamethylenediamine, hexamethylenediamine, heptamethylenediamine, octamethylenediamine, nonamethylenediamine and decamethylenediamine, preferably hexa-methylenediamine. It is further possible to use salts of the aforementioned dicarboxylic acids and diamines, especially the salt of adipic acid and hexamethylenediamine, which is known as 66 salt. The a,co-C2-Ci2-dinitrile used is preferably an aliphatic dinitrile such as 1,4-dicyanobutane (adiponitrile), 1,5-dicyanopentane, 1,6-dicyanohexane, 1,7-dicyano-heptane, 1,8-dicyanooctane, 1,9-dicyanononane, 1,10-dicyanodecane, particularly preferably adiponitrile. If desired, it is also possible to use diamines, dinitriles and aminonitriles derived from branched alkylene or arylene or alkylarylene compounds. The a,co-C5-Ci2-amino acid used can be 5-aminopentanoic acid, 6-aminohexanoic acid, 7-aminoheptanoic acid, 8-aminooctanoic acid, 9-aminononanoic acid, 10-aminodecanoic acid, 11-aminoundecanoic acid or 12-aminododecanoic acid, preferably 6-aminohexanoic acid. The aminonitrile/water mixture is heated with the aid of a heat exchanger before being introduced into the first step. The aminonitrile and the water can also be heated separately and mixed in the first step by means of mixing elements. The starting mixture is pumped in step (1) into a flow reactor containing titanium dioxide packing elements and metallic packing elements. The packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements are preferably extrudates or pellets. Particular preference is given to pellets having an average length from 5 to 20 mm and an average diameter from 3 to 6 mm. More particularly, titanium dioxide pellets having an average length of about 10 mm and a diameter of 4 mm are preferred. The titanium dioxide preferably comprises from 70 to 100% by weight of anatase and from 0 to 30% by weight of rutile. When aminonitriles are used which are essentially pure or completely pure, preference is given to using a titanium dioxide packing element composed of anatase. When impurities are present in the aminonitrile, preference is given to using a titanium dioxide packing element which comprises from 70 to 80% of anatase and from 20 to 30% by weight of rutile, particularly preferably about 70%) by weight of anatase and about 30% by weight of rutile. The catalyst preferably has a pore volume of from 0.1 to 5 ml/g, particularly preferably from 0.2 to 0.5 ml/g. The average pore diameter is preferably within the range from 0.005 to 0.1 μm, particularly preferably within the range from 0.01 to 0.06 μm. If highly viscous products are used, the average pore diameter should be large. The cutting hardness is preferably greater than 20 N, particularly preferably > 25 N. The BET surface area is preferably more than 40 m2/g, particularly preferably more than 100 m7g. If the BET surface area is smaller, the bed volume should be appropriately higher to ensure adequate catalyst activity. Particularly preferred catalysts have the following properties: 100% of anatase; 0.3 ml/g pore volume; 0.02 mm average pore diameter; 32 N cutting hardness; 116 m2/g BET surface area or 84% by weight of anatase; 16% by weight of rutile; 0.3 ml/g pore volume; 0.03 μm average pore diameter; 26 N cutting hardness; 46 m2/g BET surface area. The catalysts may be prepared from commercial powders as available for example from Degussa, Finnti or Kemira. When tungsten oxide is used, up to 40% by weight, preferably up to 30% by weight, particularly preferably from 15 to 25% by weight of the titanium dioxide is replaced by tungsten oxide. The catalysts can be prepared as described in Ertl, Knozinger, Weitkamp: "Handbook of heterogeneous catalysis", VCH Weinheim, 1997, pages 98ff. The metallic packing elements are preferably formed from corrosion-resistant metals, especially corrosion-resistant steel. The packing elements may have any suitable geometry. Raschig rings are particularly preferred. The Raschig rings preferably have a diameter from 2 to 6 mm, especially about 3 mm. The pellet size is advantageously chosen so that, on the one hand, mechanical removal of the pellets by means of filters and sieves presents no problems and, on the other, the pressure buildup due to the flow resistance caused by the increased solid-body density in the reactor remains technically manageable. The average bed density in the flow tube reactor can be set by means of a suitable ratio of packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements to metallic packing elements. The flow tube may contain mixtures of the packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements. Preferably, the packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements and the metallic packing elements form alternating layers in the flow tube. In this arrangement, a layer of packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements is preferably followed in the downstream direction by a layer of metallic packing elements. It is also possible for an alternating layer sequence of the two packing elements comprising from 3 to 20, preferably from 3 to 15, layers to be present. A comparison between a bed comprising a layer of titanium dioxide pellets followed by a layer of Raschig rings to a bed comprising Raschig rings only is shown in the drawing. Figure 1 illustrates the residence time in the form of a plot of the concentration T against the time Z in minutes for the bed comprising titanium dioxide pellets (blank boxes) and a bed composed of Raschig rings (solid circles). / The residence time distribution for the bed of the invention is significantly narrower \ than for the bed consisting exclusively of Raschig rings. The reaction conditions for step 1 are specified hereinbelow. Corresponding reaction conditions apply to step 3, which is described hereinbelow, if the bed of the invention is used as well. According to the invention, the first step (step 1) comprises heating an aminpnitrile with water at a temperature from about 90 to about 400°C, preferably from about 180 to about 310°C, in particular from about 220 to about 270°C, the pressure ranging from about 0.1 to about 15 x 106 Pa, preferably from about 1 to about 10x106 Pa, especially from about 4 to about 3 x 10 Pa. The pressure and temperature can be adjusted to each other in this stage in such a way as to obtain a liquid or a solid phase and a mixture of a liquid or a solid phase and a gaseous phase. The reaction mixture should preferably be present as a single liquid phase; that is, no gas phase should be present in the mixture. In step 1, the pressure and temperature can also be set in such a way, if desired, for the reactor to contain a gaseous and liquid phase. As part of the first step, the gaseous phase can then be separated from the liquid phase. Preferably, in the case of the two-phase procedure, the pressure chosen is greater than the vapor pressure of pure water at the bulk temperature of the reaction mixture, but less than the equilibrium vapor pressure of ammonia. In the case of the two-phase procedure it is advantageous to operate the tubular reactor in an axial upright fashion. It can be completely or partially packed with the above-described layering or mixture of packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements and metallic packing elements. In a preferred embodiment, the two-phase procedure upright reactor contains pellets of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide pellets up to the phase boundary, while the reactor volume containing the gas phase is preferably exclusively packed with metallic packing elements such as Raschig rings. According to the invention, water is used in a molar ratio of aminoalkyl nitrile to water within the range from 1:1 to 1:10, particularly preferably within the range from 1:2 to 1:8, very particularly preferably within the range from 1:2 to 1:6, and the use of water in excess, based on the aminoalkyl nitrile used, is preferred. In this embodiment, the liquid or solid phase or the mixture of a liquid or solid phase corresponds to the reaction mixture, while the gaseous phase is separated off. In the context of this step, the gaseous phase can be immediately separated from the liquid or solid phase or from the mixture of a solid or liquid phase, or the reaction mixture forming within this step can be present in two phases: liquid/gaseous, solid/gaseous or liquid-solid/gaseous. It will be appreciated that the pressure and temperature can also be adjusted relative to each other in such a way that the reaction mixture is present as a single solid or liquid phase. The removal of the gas phase can be effected by the use of stirred or unstirred separating tanks or tank batteries or by the use of evaporator apparatus, for example by means of circulatory evaporators or thin-film evaporators, such as by film extruders, or by means of annular disk reactors, which ensure an enlarged phase interface. Recirculation of the reaction mixture or the use of a loop reactor may be necessary to increase the phase interface. Furthermore, the removal of the gas phase can be furthered by the addition of water vapor or inert gas into the liquid phase. Preferably, the pressure is adjusted at a preselected temperature so that the pressure is smaller than the equilibrium vapor pressure of ammonia, but greater than the equilibrium vapor pressure of the other components in the reaction mixture at the given temperature. This way, it is possible to favor especially the removal of ammonia and thus speed up the hydrolysis of the acid amide groups. As regards the residence time of the reaction mixture in the first step, there are no restrictions whatsoever; however, it is generally set within the range from about 10 minutes to about 10 hours, preferably within the range from about 30 minutes to about 6 hours. Although there are no restrictions whatsoever concerning the degree of conversion of nitrile groups in step 1, economic reasons especially dictate that the conversion of nitrile groups in step 1 be generally not less than about 70 mol%, preferably not less than about 95 mol%, and especially within the range from about 97 to about 99 mol%, based in each case on the moles of aminonitrile used. The nitrile group conversion is customarily determined by means of IR spectroscopy (CN stretching vibration at 2247 wavenumbers), NMR or HPLC, preferably by IR spectroscopy. Nor does the invention rule out conducting the reaction in step 1 in the presence of oxygen-containing phosphorus compounds, especially phosphoric acid, phosphorous acid and hypophosphorous acid and their alkali metal and alkaline earth metal salts and ammonium salts such as Na3P04, NaH2P04, Na2HP04, NaH2P03, Na2HP03, NaH2P02, K3PO4, KH2P04, K2HP04, KH2P03, K2HP03, KH2P02, in which case the molar ratio of w-aminonitrile to phosphorus compounds is selected within the range from 0.01:1 to 1:1, preferably within the range from 0.01:1 to 0.1:1. According to the invention, the reaction mixture obtained in the first step is further reacted in step 2 at a temperature from about 150(200) to about 400(350)°C, preferably at a temperature within the range from about 300(230) to about 330(300)°C, especially within the range from about 230 to about 290(270)°C, and a pressure which is lower than the pressure in step 1. The pressure in the second step is preferably at least about 0.5 x 106 Pa lower than the pressure in step 1, and generally the pressure will be within the range from about 0.1 to about 45 x 106 Pa, preferably within the range from about 0.5 to about 15x10 Pa, especially within the range from about 0.2 to about 6 x 106 Pa. In step 2, the temperature and the pressure are chosen so as to obtain a first gas phase and a first liquid or first solid phase or a mixture of first liquid and first solid phase and the first gas phase is separated from the first liquid or first solid phase or from the mixture of first liquid and first solid phase. The first gaseous phase, which consists essentially of ammonia and water vapor, is generally removed continuously by means of a distillation apparatus, such as a distillation column. Any organic constituents of the distillate coremoved in the course of this distillation, predominantly unconverted aminonitrile, can be wholly or partly re-cycled into step 1 and/or step 2. The residence time of the reaction mixture in step 2 is not subject to any restrictions whatsoever, but is generally within the range from about 10 minutes to about 5 hours, preferably within the range from about 30 minutes to about 3 hours. The product line between the first and second steps optionally contains packing elements, such as Raschig rings or Sulzer mixing elements, which facilitate a controlled expansion of the reaction mixture into the gas phase. In step 3, the first liquid or the first solid phase or the mixture of first liquid and first solid phase is admixed with a gaseous or liquid phase comprising an aqueous medium, preferably water or water vapor. This takes place continuously. The amount of water added (as liquid) is preferably within the range from about 50 to about 1500 ml, more preferably within the range from about 100 to about 500 ml, based in each case on 1 kg of the first liquid or first solid phase or of the mixture of first liquid and first solid phase. This addition of water primarily compensates the water losses incurred in step 2 and furthers the hydrolysis of acid amide groups in the synthesis mixture. This results in a further advantage of this invention, that the mixture of the starting materials as used in step 1 can be used with a small excess of water only. The gaseous or liquid phase comprising water is preferably preheated in a heat exchanger before being introduced into step 3 and then mixed with the first liquid or the first solid phase or the mixture of first solid and first liquid phase. The reactor may optionally be fitted with mixing elements which further the mixing of the components. Step 3 can be operated at a temperature from 150 to 370°C and a pressure from 0.1 to 30 x 106Pa; if the bed of the invention is present, the conditions applying to step 1 can be employed. The pressure and temperature can be adjusted to each other in such a way that the synthesis mixture is present as a single liquid or solid phase. In another embodiment, the pressure and temperature are selected so that a liquid or a solid phase or a mixture of solid and liquid phase and also a gaseous phase are obtained. In this embodiment, the liquid or solid phase or the mixture of liquid and solid phase corresponds to the product mixture, whereas the gaseous phase is separated off. As part of this step, the gaseous phase can be separated from the liquid or solid phase or from the mixture of solid or liquid phase at once, or the synthesis mixture forming within this step can be present in two-phase form: liquid/gaseous, solid/gaseous or liquid-solid/gaseous. The pressure can be adjusted at a preselected temperature so that the pressure is smaller than the equilibrium vapor pressure of ammonia, but greater than the equili¬brium vapor pressure of the other components in the synthesis mixture at the given temperature. This way, it is possible to favor especially the removal of ammonia and thus speed up the hydrolysis of the acid amide groups. The apparatus/reactors usable in this step can be identical with those of step 1, as discussed above. The residence time in this step is likewise not subject to any restrictions, but economic reasons generally dictate a range from about 10 minutes to about 10 hours, preferably from about 60 to about 8 hours, particularly preferably from about 60 minutes to about 6 hours. The product mixture obtained in step 3 can be further processed as described below. In a preferred embodiment, the product mixture of step 3 is subjected to a postcondensation in a fourth step at a temperature from about 200 to about 350°C, preferably at a temperature from about 220 to 300°C, especially from about 250 to 270°C. Step 4 is carried out at a pressure which is below the pressure of step 3 and is preferably within the range from about 5 to 1000 x 103 Pa, more preferably within the range from about 10 to about 300 x 103 Pa. In the context of this step, the temperature and pressure are selected so as to obtain a second gas phase and a second liquid or solid phase or a mixture of second liquid and second solid phase which each comprise the polyamide. The postcondensation of step 4 is preferably carried out in such a way that the relative viscosity (measured at a temperature of 25°C and a concentration of 1 g of polymer per 100 ml in 96% strength by weight of sulfuric acid) of the polyamide assumes a value within the range from about 1.6 to about 3.5. In a preferred embodiment, any water present in the liquid phase can be expelled by means of an inert gas such as nitrogen. The residence time of the reaction mixture in step 4 depends especially on the desired relative viscosity, the temperature, the pressure and the amount of water added in step 3. If step 3 is operated as a single-phase regime, the product line between step 3 and step 4 may optionally contain packing elements, for example, Raschig rings or Sulzer mixing elements, which allow a controlled expansion of the synthesis mixture in the gas phase. In a further embodiment of the invention, step 3 may be dispensed with and the polyamide produced by carrying out steps (1), (2) and (4). This variant is preferably carried out as follows: The reaction mixture is treated in step 2 as described above or at a temperature within the range from about 220 to about 300°C and a pressure within the range from about 1 to about 7x106 Pa, the pressure in the second step being at least 0.5 x 106 Pa lower than in step 1. At the same time, the resulting first gas phase is separated from the first liquid phase. The first liquid phase obtained in step 2 is treated in step 3 as in step 1 or at a temperature within the range from about 220 to 300°C and a pressure within the range from about 10 to about 300 x 103 Pa, the resulting second, water- and ammonia-comprising gas phase being separated from the second liquid phase. Within this step, the relative viscosity (measured as defined above) of the resulting polyamide is adjusted to a desired value within the range from about 1.6 to about 3.5 through choice of temperature and residence time. The resulting second liquid phase is then conventionally discharged and, if desired, worked up. In a further preferred embodiment of the present invention, at least one of the gas phases obtained in the respective steps can be recycled into at least one of the preceding steps. It is further preferable to select the temperature and pressure in step 1 or in step 3 or in both step 1 and step 3 so as to obtain a liquid or a solid phase or a mixture of liquid and solid phase and a gaseous phase and the gaseous phase is separated off. Furthermore, in the context of the process of the invention, it is also possible to carry out a chain lengthening or branching or a combination thereof. For this purpose, polymer branching or chain-lengthening substances known to a person skilled in the art are added in the individual steps. These substances are preferably added in step 3 or 4. Usable substances are: Trifunctional amines or carboxylic acids as branching agents or crosslinkers. Examples of suitable at least trifunctional amines or carboxylic acids are described in EP-A-0 345 648. The at least trifunctional amines have at least three amino groups which are capable of reaction with carboxylic acid groups. They preferably do not have any carboxylic acid groups. The at least trifunctional carboxylic acids have at least three carboxylic acid groups which are capable of reaction with amines and which can also be present, for example, in the form of their derivatives, such as esters. The carboxylic acids preferably do not contain any amino groups capable of reaction with carboxylic acid groups. Examples of suitable carboxylic acids are trimesic acid, trimerized fatty acids, which can be prepared for example from oleic acid and can have from 50 to 60 carbon atoms, naphthalenepolycarboxylic acids, such as naphthalene-1,3,5,7-tetracarboxylic acid. The carboxylic acids are preferably defined organic compounds and not polymeric compounds. Examples of amines having at least 3 amino groups are nitrilotrialkylamine, especially nitrilotriethaneamine, dialkylenetriamines, especially diethylenetriamine, trialkylene-tetramines and tetraalkylenepentamines, the alkylene moieties preferably being ethylene moieties. Furthermore, dendrimers can be used as amines. Dendrimers preferably have the general formula I (R2N-(CH2)n)2N-(CH2)x-N((CH2)n-NR2)2 (I) where R is H or -(CH2)n-NR12, where R1 is H or -(CH2)n-NR22, where R2 is H or -(CH2)n-NR32, where R3 is H or -(CH2)n-NH2, n is an integer from 2 to 6, and x is an integer from 2 to 14. Preferably, n is 3 or 4, especially 3, and x is an integer from 2 to 6, preferably from 2 to 4, especially 2. The radicals R can also have the stated meanings independently of one another. Preferably, R is a hydrogen atom or a -(CH2)n-NH2 radical. Suitable carboxylic acids are those having from 3 to 10 carboxylic acid groups, preferably 3 or 4 carboxylic acid groups. Preferred carboxylic acids are those having aromatic and/or heterocyclic nuclei. Examples are benzyl, naphthyl, anthracene, • biphenyl, triphenyl radicals or heterocycles such as pyridine, bipyridine, pyrrole, indole, furan, thiophene, purine, quinoline, phenanthrene, porphyrin, phthalocyanine, naphthalocyanine. Preference is given to 3,5,3",5"-biphenyltetracarboxylic acid- : phthalocyanine, naphthalocyanine, 3,5,5",5"-biphenyltetracarboxylic acid, 1,3,5,7-naphthalenetetracarboxylic acid, 2,4,6-pyridinetricarboxylic acid, 3,5,3",5"-bipyrid-yltetracarboxylic acid, 3,5,3",5"-benzophenonetetracarboxylic acid, 1,3,6,8-acridinetetracarboxylic acid, particularly preferably 1,3,5-benzenetricarboxylic acid (trimesic acid) and 1,2,4,5-benzenetetracarboxylic acid. Such compounds are commercially available or can be prepared by the process described in DE-A-43 12 182. If ortho-substituted aromatic compounds are used, imide formation is preferably prevented through the choice of suitable reaction temperatures. These substances are at least trifunctional, preferably at least tetrafunctional. The number of functional groups can be from 3 to 16, preferably from 4 to 10, particularly preferably from 4 to 8. The processes of the invention are carried out using either at least trifunctional amines or at least trifunctional carboxylic acids, but not mixtures of such amines or carboxylic acids. However, small amounts of at least trifiinctional amines may be present in the trifunctional carboxylic acids, and vice versa. The substances are present in an amount from 1 to 50 mmol/g of polyamide, preferably from 1 to 35, particularly preferably 1 to 20, umol/g of polyamide. The substances are preferably present in an amount from 3 to 150, particularly preferably from 5 to 100, especially from 10 to 70, μmol of equivalents/g of polyamide. The equivalents are based on the number of functional amino groups or carboxylic acid groups. Difunctional carboxylic acids or difunctional amines are used-as chain lengtheners. These have 2 carboxylic acid groups which can be reacted with amino groups, or 2 amino groups which can be reacted with carboxylic acids. The difunctional carboxylic acids or amines, as well as the carboxylic acid groups or amino groups, do not contain any further functional groups capable of reaction with amino groups or carboxylic acid groups. Preferably, they do not contain any further functional groups. Examples of suitable difunctional amines are those which form salts with difunctional carboxylic acids. They can be linear aliphatic, such as C1.14-alkylenediamine, preferably C2-6-alkylenediamine, for example hexylenediamine. They can also be cycloaliphatic. Examples are isophoronediamine, dicycycan, laromine. Branched aliphatic diamines are likewise usable, an example being Vestamin TMD (trimethylhexamethylenediamine, from Huls AG). In addition, the diamines can also be aromatic-aliphatic, it being possible to use n-xylylenediamine, for example. Entire amines can each be substituted by Ci-12-alkyl, preferably Ci-14-alkyl, radicals on the carbon skeleton. - , t Difunctional carboxylic acids are, for example, those which form salts with difunctional diamines. They can be linear aliphatic dicarboxylic acids, which are preferably C4-20-dicarboxylic acids. Examples are adipic acid, azelaic acid, sebacic acid, suberic acid. They can also be aromatic. Examples are isophthalic acid, terephthalic acid, naphthalenedicarboxylic acid, as well as dimerized fatty acids. The difunctional basic building blocks (c) are preferably used in amounts from 1 to 55, particularly preferably from 1 to 30, especially from 1 to 15, mm/g of polyamide. According to the invention, the product mixture obtained in step 3, or the second liquid or second solid phase or the mixture of second liquid and second solid phase (from step 4) which each comprise the polyamide, preferably a polymer melt, is discharged from the reaction vessel in a conventional manner, for example by means of a pump. Subsequently, the polyamide obtained can be worked up according to conventional methods, as described for example in DE-A 43 21 683 (page 3 line 54 to page 4 line 3) at length. In a preferred embodiment, the level of cyclic dimer in the nylon-6 obtained according to the invention can be further reduced by extracting the polyamide first with an aqueous solution of caprolactam and then with water and/or subjecting it to a gas phase extraction (described in EP-A-0 284 968, for example). The low molecular weight constituents obtained in this aftertreatment, such as caprolactam, linear caprolactam oligomer and cyclic caprolactam oligomer, can be recycled into the first and/or second and/or third step. The starting mixture and the synthesis mixture can be admixed in all steps with chain regulators such as aliphatic and aromatic carboxylic and dicarboxylic acids and catalysts such as oxygen-containing phosphorus compounds in amounts within the range from 0.01 to 5% by weight, preferably within the range from 0.2 to 3% by weiglft, based on the amount of polyamide-forming monorrters and aminohitriles used. Suitable chain regulators include for example propionic acid, acetic acid, benzoic acid, terephthalic acid and triacetonediamine. Additives and fillers such as pigments, dyes and stabilizers are generally added to the synthesis mixture prior to pelletization, preferably in the second, third and fourth steps. Particular preference is given to using fillers and additives whenever the synthesis or polymer mixture will not encounter fixed bed catalysts in the rest of the processing. One or more impact-modifying rubbers may be present in the compositions as additives in amounts from 0 to 40% by weight, preferably from 1 to 30% by weight, based on the entire composition. It is possible to use, for example, customary impact modifiers which are suitable for polyamides and/or polyarylene ethers. Rubbers which enhance the toughness of polyamides generally have two essential features: they have an elastomeric portion which has a glass transition temperature of less than -10°C, preferably less than -30°C, and they contain at least one functional group which is capable of interaction with the polyamide. Suitable functional groups include for example carboxylic acid, carboxylic anhydride, carboxylic ester, carboxylic amide, carboxylic imide, amino, hydroxyl, epoxide, urethane and oxazoline groups. Examples of rubbers which enhance the toughness of the blends include for example: EP and EPDM rubbers grafted with the above functional groups. Suitable grafting reagents include for example maleic anhydride, itaconic acid, acrylic acid, glycidyl acrylate and glycidyl methacrylate. These, monomers can be grafted onto the polymer in the melt, or in solution, in the presence or absence of a free-radical initiator such as cumene hydroperoxide. The copolymers of a-olefins described under the polymers A, including especially the ethylene copolymers, may also be used as rubbers instead of polymers A and be mixed as such into the compositions of the invention. A further group of suitable elastomers are core-shell graft rubbers. These are graft rubbers which are produced in emulsion and which have at least one hard and one soft constituent. A hard constituent is customarily a polymer having a glass transition temperature of at least 25°C, while a soft constituent is a polymer having a glass transition temperature of not more than 0°C. These products have a structure made up of a core and at least one shell, the structure being the result of the order in which the monomers are added. The soft constituents are generally derived from butadiene, isoprene, alkyl acrylates, alkyl methacrylates or siloxanes and optionally further comonomers. Suitable siloxane cores can be prepared for example starting from cyclic oligomeric octamethyltetrasiloxane or tetravinyltetramethyltetrasiloxane. These can be, for example, reacted with y-mercaptopropylmethyldimethoxysilane in a ring-opening cationic polymerization, preferably in the presence of sulfonic acids, to form the soft siloxane cores. The siloxanes can also be crosslinked by, for example, conducting the polymerization reaction in the presence of silanes having hydrolyzable groups such as halogen or alkoxy groups such as tetraethoxysilane, methyltri-methoxysilane or phenyltrimethoxysilane. Suitable comonomers here include for example styrene, acrylonitrile and crosslinking or grafting monomers having more than one polymerizable double bond such as diallyl phthalate, divinylbenzene, butanediol diacrylate or triallyl (iso)cyanurate. The hard constituents are generally derived from styrene, a-methylstyrene and copolymers thereof, preferred comonomers being acrylonitrile, methacrylonitrile and methyl methacrylate. Preferred core-shell graft rubbers have a soft core and a hard shell or a hard core, a first 30ft shell and at least one further hard shell. The incorporation of functional groups such as carbonyl, carboxylic acid, acid anhydride, acid amide, acid imide, carboxylic esters, amino, hydroxyl, epoxy, oxazoline, urethane, urea, lactam or halobenzyl groups is here preferably effected by the addition of suitably functionalized monomers during the polymerization of the last shell. Suitable functionalized monomers include for example maleic acid, maleic anhydride, mono-or diesters or maleic acid, tert-butyl (meth)acrylate, acrylic acid, glycidyl (meth)acrylate and vinyloxazoline. The proportion of monomers having functional groups is generally within the range from 0.1 to 25% by weight, preferably within the range from 0.25 to 15% by weight, based on the total weight of the core-shell graft rubber. The weight ratio of soft to hard constituents is generally within the range from 1:9 to 9:1, preferably within the range from 3:7 to 8:2. Such rubbers, which enhance the toughness of polyamides, are known per se and described in EP-A-0 208 187, for example. A further group of suitable impact modifiers are thermoplastic polyester elastomers. Polyester elastomers are segmented copolyetheresters containing long-chain segments, generally derived from poly(alkylene) ether glycols, and short-chain segments, derived from low molecular weight diols and dicarboxylic acids. Such products are known per se and are described in the literature, for example in US 3,651,014. Corresponding products are also commercially available under the names of Hytrel® (Du Pont), Arnitel® (Akzo) and Pelprene® (Toyobo Co. Ltd.). It will be appreciated that it is also possible to use mixtures of different rubbers. As further additives there may be mentioned for example processing aids, stabilizers and oxidation retardants, agents against thermal decomposition and decomposition by ultraviolet light, lubricating and demolding agents, flame retardants, dyes and pigments and plasticizers. The proportion thereof is generally up to 40%, preferably up to 15%o, by weight, based on the total weight of the composition. Pigments and dyes are generally present in amounts of up to 4%, preferably from 0.5 to 3.5%o, especially from 0.5 to 3%, by weight. The pigments for coloring thermoplastics are commonly known, see for example R. Gachter and H. Muller, Taschenbuch der Kunststoffadditive, Carl Hanser Verlag, 1983, pages 494 to 510. The first preferred group of pigments to be mentioned are white pigments such as zinc oxide, zinc sulfide, lead white (2 PbC03 • Pb(OH)2), lithopone, antimony white and titanium dioxide. Of the two most common crystal polymorphs (rutile and anatase) of titanium dioxide, the rutile form is preferred for use as white pigment for the molding compositions of the invention. Black pigments which can be used according to the invention are iron oxide black (Fe3O4), spinel black (Cu(Cr,Fe)2O4), manganese black (mixture of manganese dioxide, silicon dioxide and iron oxide), cobalt black and antimony black and also, particularly preferably, carbon black, which is usually used in the form of furnace or gas black (see G. Benzing, Pigmente fur Anstrichmittel, Expert-Verlag (1988), p. 78ff). It will be appreciated that inorganic color pigments such as chromium oxide green or organic color pigments such as azo pigments and phthalocyanines can be used according to the invention to obtain certain hues. Such pigments are generally commercially available. It can further be of advantage to use the abovementioned pigments or dyes in a mixture, for example carbon black with copper phthalocyanines, since this generally facilitates the dispersion of color in the thermoplastic. Oxidation retardants and thermal stabilizers which can be added to the thermoplastic compositions of the invention include for example halides of metals of group I of the periodic table, e.g., sodium halides, potassium halides, lithium halides, optionally in conjunction with copper(I) halides, for example chlorides, bromides 6r iodides. The halides, especially of copper, may also contain electron-rich p-ligands. Examples of such copper complexes are copper halide complexes with triphenylphosphine, for example. It is further possible to use zinc fluoride and zinc chloride. Other possibilities are sterically hindered phenols, hydroquinones, substituted represen¬tatives of this group, secondary aromatic amines, optionally in conjunction with phosphorus-containing acids and salts thereof, and mixtures of these compounds, preferably in a concentration up to 1% by weight, based on the weight of the mixture. Examples of UV stabilizers are various substituted resorcinols, salicylates, benzo-triazoles and benzophenones, which are generally used in amounts of up to 2% by weight. Lubricating and demolding agents, which are generally included in the thermoplastic material in amounts of up to 1% by weight, are stearic acid, stearyl alcohol, alkyl stearates and N-alkylstearamides and also esters of pentaerythritol with long-chain fatty acids. It is also possible to use salts of calcium, of zinc or of aluminum of stearic acid and also dialkyl ketones, for example distearyl ketone. The present invention further provides a polyamide producible by any of the foregoing processes. The examples which follow illustrate the invention. Examples Measurement of residence time distribution The effect of the various mixing elements on the residence time distribution is investigated in a glass tubular reactor. The glass cylinder, which has the same length (100 cm) and the same internal diameter (3.6 cm) as the tubular reactor used for ACN direct polymerization, is fitted with the corresponding mixing elements for this purpose. The mixing elements used are 3 mm Raschig rings or TiO2 extrudates (diameter 4 mm, length 5-10 mm). Water is pumped through the flow tube at a rate of 600 g/h using an HPLC pump. Methylene blue (0.05% strength) is used as tracer. The tracer solution is fed to the reactor inlet, again at a rate of 600 g/h, via the main feed line. During the injection of the tracer solution, which takes 1 minute, the feed of the tracer-free liquid is interrupted. Samples are taken at the reactor outlet at intervals within the range from 3 to 5 minutes. The tracer concentration of the samples is determined via absorption spectroscopy. Characterization of the residence time distribution through calculation of the Bodenstein number The purpose of the analysis is to characterize the measured residence time distributions, so that the effect of the mixing elements can be compared. The average residence time t" and the Bodenstein number Bo, which is a measure of the width, and shape of distribution time curves, are suitable t parameters here for demonstrating the dependence of the residence time behavior on the mixing element. The measured concentration (T) - time profiles (Z) (T in arbitrary units, Z in minutes) of the tracers display distinct departures from a Gaussian distribution, evidence of pronounced axial dispersion. It therefore appears sensible to employ the dispersion model for real reactors, which is described for example in Octave Levenspiel, Chemical Engineering, 2nd Edition, John Wiley & Sons, New York (1962), for describing the response function means measured. This model introduces a diffuse term with the dispersion coefficient D which takes account of the degree of axial mixing. The analytic solution of the dispersion model describes the dependence of the response function C on the dimensionless quotient Bo, the Bodenstein number. where u is the hydrodynamic flow velocity, L is the path length, D is the dispersion coefficient and D is the hydrodynamic residence time. The shape of the residence time curves depends on the axial dispersion and is thus a function of the Bodenstein number. The larger the Bodenstein number, the more the flow in the reactor corresponds to an ideal plug flow. By fitting equation (1) to the normalized response functions, the appropriate values are obtained for the (fitting) parameters Bo and T. Catalyst preparation Catalyst 1 Beta-zeolite powder The catalyst used was a beta-zeolite from Uetikon (Zeokat-Beta) having the following composition: Si02 = 91%, A1203 = 7.8%, Na20 = 0.5%, K20 = 0.7%, BET surface area = 700 m2/g, pore size in A = 7.6 x 6.7; 5.5 x 5.5, particle size 0.2-0.5 mm. Catalyst 2 Beta-zeolite extrudates 220 g of P-zeolite from Example 1 were kneaded with 5% of Walocel® and 230 g of water for 45 minutes. The material was then molded under a pressure of 70 bar into 2 mm extrudates. These were dried at 110°C and calcined at 500°C for 16 h. 195 g of these extrudates were exchanged with 3 liters of 20%> strength NH4CI solution at 80°C for 2 h and then washed with 10 1 of water. Thereafter a second exchange was effected again with 3 1 of 20%) strength NH4CI solution at 80°C/2 h and the product was washed Cl-free. Drying at 110°C was followed by 5 h of calcination at 500°C. Catalyst 3 Sheet-silicate type K10® K10® is an acid-treated montmorillonite from Sud-Chemie. It has a BET surface area of 180-220 m7g and an ion exchange equivalent of 40-50 meq/100 g. Catalysts 4 and 5 TiCh extrudates of 100% and 84% anatase, respectively Preparation is in line with the description in Ertl, Knozinger, Weitkamp: "Handbook of heterogeneous catalysis", VCH Weinheim, 1997; page 98ff. The T1O2 polymorphs described as particularly preferred in the preceding description were mixed with water, silica sol and glycerol, extruded and calcined at 550°C. Catalyst 6 Titanium dioxide/tungsten oxide catalyst The catalyst used was obtained by intimately mixing the commercially available titanium dioxide VKR 611 (from Sachtleben) with tungsten oxide and subsequent extrusion as per Example 2 or 4. It has the following specification: 20% by weight of WO3, 80% by weight of TiO?; BET surface area = 73 m2/g, total acidity (pKa = 6.8) = 0.56 mmol/g; total acidity (pKa=-3) = 0.035mmol/g. Inventive Examples 1-3 The table shows the improvement in the residence time distribution, i.e., the reduction in axial backmixing, obtained through the use of TiO2 pellets (catalyst 4: extrudates 4 mm in thickness and about 7 mm in average length). Compared with the pure TiO2 bed (Comparative Example CI) and the T1O2 free bed of the Raschig ring packing elements (Comparative Example C2), the residence time distribution of Inventive Examples 1 and 2 is narrower, i.e., the Bodenstein number Bo is larger. The result measured for Inventive Example 1, in which T1O2 pellets and Raschig rings are used as packing elements in the reactor, and of Comparative Example C2 with (exclusively) Raschig rings is depicted in Figure 1 together with the calculated residence time curves. The alternating beds in the tubular reactor are characterized by the layer thickness and the packing elements used. The stated order of the beds corresponds to the bed sequence in the reactor in the direction of flow, i.e., in the upward direction. We claim: 1. A continuous process for producing a polyamide by reacting at least one aminonitrile with water, comprising the following steps: (1) reacting at least one aminonitrile with water in a molar ratio of from 1:1 to 1:10 at a temperature from 90 to 400°C and a pressure from 0.1 to 15 x 106 Pa in a flow tube containing packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements and metallic packing elements wherein the packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements and the metallic packing elements form alternating layers in the flow tube, to obtain a reaction mixture, (2) further reacting the reaction mixture at from 150 to 400°C and a pressure which is lower than the pressure in step 1, the temperature and pressure being selected so as to obtain a first gas phase and a first liquid or a first solid phase or a mixture of first solid and first liquid phase, and the first gas phase is separated from the first liquid or first solid phase or the mixture of first liquid and first solid phase, and (3) admixing the first liquid or the first solid phase or the mixture of first liquid and first solid phase with a gaseous or liquid phase comprising water at a temperature from 150 to 370°C and a pressure from 0.1 to 30 x 10 Pa to obtain a product mixture. 2. The process as claimed in claim 1, wherein step (3) is performed in a flow tube containing packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements and metallic packings wherein the packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements and the metallic packing elements form alternating layers in the flow tube. 3. The process as claimed in claim 1 or 2, further comprising the following step: postcondensing the product mixture at a temperature from 200 to 350°C and a pressure which is lower than the pressure in step 3, the temperature and pressure being selected so as to obtain a second, water- and ammonia-comprising gas phase and a second liquid or second solid phase or a mixture of second liquid and second solid phase, which each comprise the polyamide. 4. The continuous process for producing a polyamide by reacting at least one aminonitrile with water, comprising the steps of reacting at least one aminonitrile with water in a molar ratio of from 1:1 to 1:10 at a temperature from 90 to 400°C and a pressure from 0.1 to 15 x 106 Pa in a flow tube containing packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements and metallic packing elements wherein the packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements and the metallic packing elements form alternating layers in the flow tube, to obtain a reaction mixture, further reacting the reaction mixture at from 150 to 400°C and a pressure which is lower than the pressure in step 1, the temperature and pressure being selected so as to obtain a first gas phase and a first liquid or a first solid phase or a mixture of first solid and first liquid phase, and the first gas phase is separated from the first liquid or first solid phase or the mixture of first liquid and first solid phase, and postcondensing the first liquid or the first solid phase or the mixture of first liquid and first solid phase at a temperature from 200 to 350°C and a pressure which is lower than the pressure in step 2, the temperature and pressure being selected so as to obtain a second, water- and ammonia-comprising gas phase and a second liquid or second solid phase or a mixture of second liquid and second solid phase, which each comprise the polyamide. 5. The process as claimed in any of claims 1 to 4, wherein the temperature and pressure in step 1 or in step 3 or both in step 1 and step 3 are selected so as to obtain a liquid or a solid phase or a mixture of liquid and solid phase and a gaseous phase and the gaseous phase is separated off. 6. The process as claimed in any of claims 1 to 5, wherein the titanium dioxide packing elements consist of Ti02 comprising from 70 to 100% by weight of anatase and from 0 to 30% by weight of rutile and in which up to 40% by weight of the titanium dioxide may be replaced by tungsten oxide. 7. The process as claimed in any of claims 1 to 6, wherein at least one of the gas phases obtained in the respective steps is recycled into at least one of the preceding steps. 8. The process as claimed in any of claims 1 to 7, wherein the aminonitrile reacted is an α -aminoalkyl nitrile having an alkylene moiety (-CH2-) of from 4 to 12 carbon atoms or an aminoalkylaryl nitrile having from 8 to 13 carbon atoms. 9. The process as claimed in any of claims 1 to 8 for the preparation of copolyamides, branched or chain lengthened polyamide a mixture consisting of: from 50 to 99.99% by weight of 6-aminocapronitrile, from 0.01 to 50% by weight of at least one dicarboxylic acid selected from the group consisting of aliphatic C4-Cio-a,G)-di-carboxylic acids, aromatic C8-Ci2- dicarboxylic acids and C5-Q-cycloalkanedicarboxylic acids, from 0 to 50% by weight of an a,co-diamine having 4-10 carbon atoms, from 0 to 50% by weight of an a,co-C2-Ci2-dinitrile, from 0 to 50% by weight of an aα -C5-C12-amino acid or of the corresponding lactam, and from 0 to 10% by weight of at least one inorganic acid or salt thereof, the individual weight percentages adding up to 100% is reacted. 10. A continuous process for producing a polyamide substantially as herein described with reference to the accompanying drawings.

Full Text

Continuous process for producing polyamides
from aminonitriles
The present invention relates to a continuous process for producing polyamides from aminonitriles and water at elevated temperature and elevated pressure.
US 4,629,776 describes a catalytic process for producing polyamides from w-aminonitriles such as w-amino-capronitrile (ACN). ACN is reacted with water in the presence of a catalytic amount of an oxidized sulfur compound as catalyst. Sulfuric acid is an example of the catalyst used.
US 4,568,736 describes a similar catalytic process for producing polyamides. The catalyst used in this case is an oxygen-containing phosphorus compound, phosphoric acid or a phosphonic acid.
Complete removal of catalyst is virtually impossible in either process. The presence of catalyst in the polymer can hinder the building of high molecular weight polymers and compromise later processing operations, for example spinning. Moreover, the level of volatiles in the polymers obtained is high, so that the polyamides are difficult to process.
EP-A-0 479 306 describes the production of polyamides from w-arnjnonitriles. The w-aminonitriles are reacted with water in the presence of an oxygen-containing

phosphorus compound as catalyst. Once a reaction temperature from 200 to 260°C has been obtained, ammonia and water are continuously removed by decompressing and at the same time water is continuously added, the pressure being selected within the range from 14 to 24 x 106Pa (14-24 bar).
DE-A-43 39 648 relates to a process for producing caprolactam by reacting aminocarbonitriles with water in the liquid phase using heterogeneous catalysts. Suitable heterogeneous catalysts include acidic, basic or amphoteric oxides of the elements of main groups 2, 3 and 4 of the Periodic Table. Titanium dioxide can be used, for example. The catalyst is used in the form of extrudates, for example.
A continuous reaction requires intensive transverse mixing within the tubular reactors used, to even out concentration and temperature gradients. In addition, any axial backmixing should be as low as possible. Only effective suppression of axial backmixing, or axial dispersion, makes it possible to achieve a plug flow profile which guarantees a narrow residence time distribution and a defined equal residence time for all volume elements in the tubular reactor.
It is an object of the present invention to provide a continuous process for producing polyamides from aminonitriles using a tubular reactor which substan¬tially prevents backmixing and provides a narrow residence time distribution. In addition, improved reaction conditions, a lower temperature and lower pressure shall be obtainable.
We have found that this object is achieved according to the invention by a continuous process for producing a polyamide by reacting at least one aminonitrile with water, comprising the following steps:

(1) reacting at least one aminonitrile with water at a temperature from(90 to 400°C and a pressure from 0.1 to 15 x 106 Pa in a flow tube containing packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements and metallic packing elements to obtain a reaction mixture,
(2) further reacting the reaction mixture at from 150 to 400°C and a pressure which is lower than the pressure in step 1, the temperature and pressure )
being selected so as to obtain a first gas phase and a first liquid or a first ; -." solid phase or a mixture of first solid and first liquid phase, and the first gas \ phase is separated from the first liquid or first solid phase or the mixture of first liquid and first solid phase, and
(3) admixing the first liquid or the first solid phase or the mixture of first liquid
and first solid phase with a gaseous or liquid phase comprising water at a
temperature from 150 to 370°C and a pressure from 0.1 to 30 x 106 Pa to
obtain a product mixture.
The present invention further provides a continuous process for producing a polyamide by reacting at least one aminonitrile with water, comprising the following steps:
(1) reacting at least one aminonitrile with water at a temperature from(l90 to }
400°C and a pressure from 0.1 to 15 x 106 Pa in a flow tube containing
packing elements of a Bronsted acid catalyst selected from beta-zeolite,
sheet-silicate or titanium dioxide packing elements and metallic packing
elements to obtain a reaction mixture,
(2) * further reacting the reaction mixture at from 150 to 400°C and a pressure
which is lower than the pressure in step 1, the temperature and pressure being selected so as to obtain a first gas phase and a first liquid or a first solid phase or a mixture of first solid and first liquid phase, and the first gas

phase is separated from the first liquid or first solid phase or the mixture of first liquid and first solid phase, and
(3) admixing the first liquid or the first solid phase or the mixture of first liquid
and first solid phase with a gaseous or liquid phase comprising water at a
temperature from 150 to 370°C and a pressure from 0.1 to 30 x 106 Pa in a
flow tube containing packing elements of a Bronsted acid catalyst selected,
from beta-zeolite, sheet-silicate or titanium dioxide packing elements and
metallic packings to obtain a product mixture.
The foregoing processes preferably further comprise the following step:
(4) postcondensing the first liquid or the first solid phase or the mixture of first
liquid and first solid phase at a temperature from 200 to 350°C and a
pressure which is lower than the pressure in step 3, the temperature and
pressure being selected so as to obtain a second, water- and ammonia-
comprising gas phase and a second liquid or second solid phase or a
mixture of second liquid and second solid phase, which each comprise the
polyamide.
The present invention further provides a continuous process for producing a polyamide by reacting at least one aminonitrile with water, comprising the following steps:
(1) reacting at least one aminonitrile with water at a temperature from 90 to 300°C and a pressure from 0.1 to 15 x 106 Pa in a flow tube containing packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements and metallic packing elements to obtain a reaction mixture,

(2) further reacting the reaction mixture at from 150 to 400°C and a pressure
which is lower than the pressure in step 1, the temperature and pressure
being selected so as to obtain a first gas phase and a first liquid or a first I
solid phase or a mixture of first solid and first liquid phase, and the first gas
phase is separated from the first liquid or first solid phase or the mixture of
first liquid and first solid phase, and "
(4) postcondensing the first liquid or the first solid phase or the mixture of first liquid and first solid phase at a temperature from 200 to 350°C and a pressure which is lower than the pressure in step 3, the temperature and pressure being selected so as to obtain a second, water- and ammonia-comprising gas phase and a second liquid or second solid phase or a mixture of second liquid and second solid phase, which each comprise the polyamide.
The inventors have found that the use of a combination of titanium dioxide packing
elements and metallic packing elements in flow tubes (also known as tubular
■ reactors) leads to a narrow residence time distribution of the reaction mixture in the
tube. In addition it is possible to lower the reaction temperature required for
converting the reaction mixture and the reaction pressure in the flow tubes. The
" " . i
process of the invention thus leads to an improvement in product homogeneity and ;
product quality while at the same time reducing the energy input into the reaction ,
mixture.
The principle of the process of the invention is described in prior DE-A-197 09 390, unpublished at the priority date of the present invention.
An aminonitrile is reacted with water in the flow tube in a first step, subjected to a partial hydro lytic polymerization and further processed in subsequent reaction steps. The overall process comprises 3 or 4 steps. The flow tubes equipped according to the invention can be used in steps (1) and (3).

The aminonitrile in the mixture can be in principle any aminonitrile, i.e., any \ compound having both at least one amino group and at least one nitrile group, (w-) Aminonitriles are preferred, especially co-aminoalkyl nitriles having from 4 to 12
5 carbon atoms, more preferably 4 to 9 carbon atoms, in the alkylene moiety, or an aminoalkylaryl nitrile having from 8 to 13 carbon atoms, preferred aminoalkylaryl nitriles being aminoalkylaryl nitriles which have an alkylene group of at least one carbon atom between the aromatic unit and the amino and nitrile group. Especially preferred aminoalkylaryl nitriles are those which have the amino group and nitrile ;
) group in the 1,4 position relative to each other.
The co-aminoalkyl nitrile used is preferably a linear co-aminoalkyl nitrile in which the alkylene moiety (-CH2-) preferably contains from 4 to 12 carbon atoms, more preferably from 4 to 9 carbon atoms, such as 6-amino-l-cyanopentane (6- | aminocapronitrile), 7-amino-l-cyanohexane, 8-amino-l-cyanoheptane, 9-amino-l- ! cyanooctane, 10-amino-1 -cyanononane, particularly preferably 6-aminocapronitrile. j
6-Aminocapronitrile is customarily obtained by hydrogenation of adiponitrile according to known methods, described for example in DE-A 836,938, DE-A 848,654 or US 5,151,543.
Of course, it is also possible to use mixtures of a plurality of aminonitriles or mixtures of an aminonitrile with further comonomers, such as caprolactam or the below-defined mixture.
In a particular embodiment, especially if copolyamides or branched or chain-lengthened polyamides are to be prepared, the following mixture is used instead of pure 6-aminocapronitrile:

from 50 to 99.99, preferably from 80 to 90, % by weight of 6-aminocapronitrile,
from 0.01 to 50, preferably from 1 to 30, % by weight of at least one dicarboxylic acid selected from the group consisting of aliphatic C4-C10-a,co-dicarboxylic acids, aromatic C5-C12-dicarboxylic acids and C5-C5-cycloalkanedicarboxylic acids,
from 0 to 50, preferably from 0.1 to 30, % by weight of an a,co-diamine having from 4 to 10 carbon atoms,
from 0 to 50, preferably from 0 to 30, % by weight of an a,co-C2-Ci2-dinitrile, and
from 0 to 50, preferably from 0 to 30, % by weight of an a,co-C5-Ci2-amino acid or of the corresponding lactam,
from 0 to 10% by weight of at least one inorganic acid or salt thereof,
the individual weight percentages adding up to 100%.
Suitable dicarboxylic acids include aliphatic C4-C10-ct,-dicarboxylic acids such as succinic acid, glutaric acid, adipic acid, pimelic acid, suberic acid, azelaic acid, sebacic acid, preferably adipic acid and sebacic acid, particularly preferably adipic acid, and aromatic Cs-Ci2-dicarboxylic acids such as terephthalic acid and also C5-C8-cycloalkanedicarboxylic acids such as cyclo-hexanedicarboxylic acid.
Suitable a,co-diamines having from 4 to 10 carbon atoms include tetramethylene-diamine, pentamethylenediamine, hexamethylenediamine, heptamethylenediamine, octamethylenediamine, nonamethylenediamine and decamethylenediamine, preferably hexa-methylenediamine.
It is further possible to use salts of the aforementioned dicarboxylic acids and diamines, especially the salt of adipic acid and hexamethylenediamine, which is known as 66 salt.

The a,co-C2-Ci2-dinitrile used is preferably an aliphatic dinitrile such as 1,4-dicyanobutane (adiponitrile), 1,5-dicyanopentane, 1,6-dicyanohexane, 1,7-dicyano-heptane, 1,8-dicyanooctane, 1,9-dicyanononane, 1,10-dicyanodecane, particularly preferably adiponitrile.
If desired, it is also possible to use diamines, dinitriles and aminonitriles derived from branched alkylene or arylene or alkylarylene compounds.
The a,co-C5-Ci2-amino acid used can be 5-aminopentanoic acid, 6-aminohexanoic acid, 7-aminoheptanoic acid, 8-aminooctanoic acid, 9-aminononanoic acid, 10-aminodecanoic acid, 11-aminoundecanoic acid or 12-aminododecanoic acid, preferably 6-aminohexanoic acid.
The aminonitrile/water mixture is heated with the aid of a heat exchanger before being introduced into the first step. The aminonitrile and the water can also be heated separately and mixed in the first step by means of mixing elements. The starting mixture is pumped in step (1) into a flow reactor containing titanium dioxide packing elements and metallic packing elements.
The packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements are preferably extrudates or pellets. Particular preference is given to pellets having an average length from 5 to 20 mm and an average diameter from 3 to 6 mm. More particularly, titanium dioxide pellets having an average length of about 10 mm and a diameter of 4 mm are preferred. The titanium dioxide preferably comprises from 70 to 100% by weight of anatase and from 0 to 30% by weight of rutile. When aminonitriles are used which are essentially pure or completely pure, preference is given to using a titanium dioxide packing element composed of anatase. When impurities are present in the aminonitrile, preference is given to using a titanium dioxide packing element which comprises from 70 to 80% of anatase and from 20 to 30% by weight of rutile, particularly preferably about 70%) by weight of anatase and about

30% by weight of rutile. The catalyst preferably has a pore volume of from 0.1 to 5 ml/g, particularly preferably from 0.2 to 0.5 ml/g. The average pore diameter is preferably within the range from 0.005 to 0.1 μm, particularly preferably within the range from 0.01 to 0.06 μm. If highly viscous products are used, the average pore diameter should be large. The cutting hardness is preferably greater than 20 N, particularly preferably > 25 N. The BET surface area is preferably more than 40 m2/g, particularly preferably more than 100 m7g. If the BET surface area is smaller, the bed volume should be appropriately higher to ensure adequate catalyst activity. Particularly preferred catalysts have the following properties: 100% of anatase; 0.3 ml/g pore volume; 0.02 mm average pore diameter; 32 N cutting hardness; 116 m2/g BET surface area or 84% by weight of anatase; 16% by weight of rutile; 0.3 ml/g pore volume; 0.03 μm average pore diameter; 26 N cutting hardness; 46 m2/g BET surface area. The catalysts may be prepared from commercial powders as available for example from Degussa, Finnti or Kemira. When tungsten oxide is used, up to 40% by weight, preferably up to 30% by weight, particularly preferably from 15 to 25% by weight of the titanium dioxide is replaced by tungsten oxide. The catalysts can be prepared as described in Ertl, Knozinger, Weitkamp: "Handbook of heterogeneous catalysis", VCH Weinheim, 1997, pages 98ff.
The metallic packing elements are preferably formed from corrosion-resistant metals, especially corrosion-resistant steel. The packing elements may have any suitable geometry. Raschig rings are particularly preferred. The Raschig rings preferably have a diameter from 2 to 6 mm, especially about 3 mm.
The pellet size is advantageously chosen so that, on the one hand, mechanical removal of the pellets by means of filters and sieves presents no problems and, on the other, the pressure buildup due to the flow resistance caused by the increased solid-body density in the reactor remains technically manageable. The average bed density in the flow tube reactor can be set by means of a suitable ratio of packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements to metallic packing elements. The flow tube may contain mixtures

of the packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements. Preferably, the packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements and the metallic packing elements form alternating layers in the flow tube. In this arrangement, a layer of packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements is preferably followed in the downstream direction by a layer of metallic packing elements. It is also possible for an alternating layer sequence of the two packing elements comprising from 3 to 20, preferably from 3 to 15, layers to be present.
A comparison between a bed comprising a layer of titanium dioxide pellets followed by a layer of Raschig rings to a bed comprising Raschig rings only is shown in the drawing.
Figure 1 illustrates the residence time in the form of a plot of the concentration T against the time Z in minutes for the bed comprising titanium dioxide pellets (blank boxes) and a bed composed of Raschig rings (solid circles).
/ The residence time distribution for the bed of the invention is significantly narrower \ than for the bed consisting exclusively of Raschig rings.
The reaction conditions for step 1 are specified hereinbelow. Corresponding reaction conditions apply to step 3, which is described hereinbelow, if the bed of the invention is used as well.
According to the invention, the first step (step 1) comprises heating an aminpnitrile with water at a temperature from about 90 to about 400°C, preferably from about 180 to about 310°C, in particular from about 220 to about 270°C, the pressure ranging from about 0.1 to about 15 x 106 Pa, preferably from about 1 to about 10x106 Pa,

especially from about 4 to about 3 x 10 Pa. The pressure and temperature can be adjusted to each other in this stage in such a way as to obtain a liquid or a solid phase and a mixture of a liquid or a solid phase and a gaseous phase. The reaction mixture should preferably be present as a single liquid phase; that is, no gas phase should be present in the mixture.
In step 1, the pressure and temperature can also be set in such a way, if desired, for the reactor to contain a gaseous and liquid phase. As part of the first step, the gaseous phase can then be separated from the liquid phase. Preferably, in the case of the two-phase procedure, the pressure chosen is greater than the vapor pressure of pure water at the bulk temperature of the reaction mixture, but less than the equilibrium vapor pressure of ammonia. In the case of the two-phase procedure it is advantageous to operate the tubular reactor in an axial upright fashion. It can be completely or partially packed with the above-described layering or mixture of packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements and metallic packing elements. In a preferred embodiment, the two-phase procedure upright reactor contains pellets of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide pellets up to the phase boundary, while the reactor volume containing the gas phase is preferably exclusively packed with metallic packing elements such as Raschig rings.
According to the invention, water is used in a molar ratio of aminoalkyl nitrile to water within the range from 1:1 to 1:10, particularly preferably within the range from 1:2 to 1:8, very particularly preferably within the range from 1:2 to 1:6, and the use of water in excess, based on the aminoalkyl nitrile used, is preferred.
In this embodiment, the liquid or solid phase or the mixture of a liquid or solid phase corresponds to the reaction mixture, while the gaseous phase is separated off. In the context of this step, the gaseous phase can be immediately separated from the liquid or solid phase or from the mixture of a solid or liquid phase, or the reaction mixture forming within this step can be present in two phases: liquid/gaseous, solid/gaseous

or liquid-solid/gaseous. It will be appreciated that the pressure and temperature can also be adjusted relative to each other in such a way that the reaction mixture is present as a single solid or liquid phase.
The removal of the gas phase can be effected by the use of stirred or unstirred separating tanks or tank batteries or by the use of evaporator apparatus, for example by means of circulatory evaporators or thin-film evaporators, such as by film extruders, or by means of annular disk reactors, which ensure an enlarged phase interface. Recirculation of the reaction mixture or the use of a loop reactor may be necessary to increase the phase interface. Furthermore, the removal of the gas phase can be furthered by the addition of water vapor or inert gas into the liquid phase.
Preferably, the pressure is adjusted at a preselected temperature so that the pressure is smaller than the equilibrium vapor pressure of ammonia, but greater than the equilibrium vapor pressure of the other components in the reaction mixture at the given temperature. This way, it is possible to favor especially the removal of ammonia and thus speed up the hydrolysis of the acid amide groups.
As regards the residence time of the reaction mixture in the first step, there are no restrictions whatsoever; however, it is generally set within the range from about 10 minutes to about 10 hours, preferably within the range from about 30 minutes to about 6 hours.
Although there are no restrictions whatsoever concerning the degree of conversion of nitrile groups in step 1, economic reasons especially dictate that the conversion of nitrile groups in step 1 be generally not less than about 70 mol%, preferably not less than about 95 mol%, and especially within the range from about 97 to about 99 mol%, based in each case on the moles of aminonitrile used.

The nitrile group conversion is customarily determined by means of IR spectroscopy (CN stretching vibration at 2247 wavenumbers), NMR or HPLC, preferably by IR spectroscopy.
Nor does the invention rule out conducting the reaction in step 1 in the presence of oxygen-containing phosphorus compounds, especially phosphoric acid, phosphorous acid and hypophosphorous acid and their alkali metal and alkaline earth metal salts and ammonium salts such as Na3P04, NaH2P04, Na2HP04, NaH2P03, Na2HP03, NaH2P02, K3PO4, KH2P04, K2HP04, KH2P03, K2HP03, KH2P02, in which case the molar ratio of w-aminonitrile to phosphorus compounds is selected within the range from 0.01:1 to 1:1, preferably within the range from 0.01:1 to 0.1:1.
According to the invention, the reaction mixture obtained in the first step is further reacted in step 2 at a temperature from about 150(200) to about 400(350)°C, preferably at a temperature within the range from about 300(230) to about 330(300)°C, especially within the range from about 230 to about 290(270)°C, and a pressure which is lower than the pressure in step 1. The pressure in the second step is preferably at least about 0.5 x 106 Pa lower than the pressure in step 1, and generally the pressure will be within the range from about 0.1 to about 45 x 106 Pa, preferably within the range from about 0.5 to about 15x10 Pa, especially within the range from about 0.2 to about 6 x 106 Pa.
In step 2, the temperature and the pressure are chosen so as to obtain a first gas phase and a first liquid or first solid phase or a mixture of first liquid and first solid phase and the first gas phase is separated from the first liquid or first solid phase or from the mixture of first liquid and first solid phase.
The first gaseous phase, which consists essentially of ammonia and water vapor, is generally removed continuously by means of a distillation apparatus, such as a distillation column. Any organic constituents of the distillate coremoved in the course

of this distillation, predominantly unconverted aminonitrile, can be wholly or partly re-cycled into step 1 and/or step 2.
The residence time of the reaction mixture in step 2 is not subject to any restrictions whatsoever, but is generally within the range from about 10 minutes to about 5 hours, preferably within the range from about 30 minutes to about 3 hours.
The product line between the first and second steps optionally contains packing elements, such as Raschig rings or Sulzer mixing elements, which facilitate a controlled expansion of the reaction mixture into the gas phase. In step 3, the first liquid or the first solid phase or the mixture of first liquid and first solid phase is admixed with a gaseous or liquid phase comprising an aqueous medium, preferably water or water vapor. This takes place continuously. The amount of water added (as liquid) is preferably within the range from about 50 to about 1500 ml, more preferably within the range from about 100 to about 500 ml, based in each case on 1 kg of the first liquid or first solid phase or of the mixture of first liquid and first solid phase. This addition of water primarily compensates the water losses incurred in step 2 and furthers the hydrolysis of acid amide groups in the synthesis mixture. This results in a further advantage of this invention, that the mixture of the starting materials as used in step 1 can be used with a small excess of water only.
The gaseous or liquid phase comprising water is preferably preheated in a heat exchanger before being introduced into step 3 and then mixed with the first liquid or the first solid phase or the mixture of first solid and first liquid phase. The reactor may optionally be fitted with mixing elements which further the mixing of the components.
Step 3 can be operated at a temperature from 150 to 370°C and a pressure from 0.1 to 30 x 106Pa; if the bed of the invention is present, the conditions applying to step 1 can be employed.

The pressure and temperature can be adjusted to each other in such a way that the synthesis mixture is present as a single liquid or solid phase. In another embodiment, the pressure and temperature are selected so that a liquid or a solid phase or a mixture of solid and liquid phase and also a gaseous phase are obtained. In this embodiment, the liquid or solid phase or the mixture of liquid and solid phase corresponds to the product mixture, whereas the gaseous phase is separated off. As part of this step, the gaseous phase can be separated from the liquid or solid phase or from the mixture of solid or liquid phase at once, or the synthesis mixture forming within this step can be present in two-phase form: liquid/gaseous, solid/gaseous or liquid-solid/gaseous.
The pressure can be adjusted at a preselected temperature so that the pressure is smaller than the equilibrium vapor pressure of ammonia, but greater than the equili¬brium vapor pressure of the other components in the synthesis mixture at the given temperature. This way, it is possible to favor especially the removal of ammonia and thus speed up the hydrolysis of the acid amide groups.
The apparatus/reactors usable in this step can be identical with those of step 1, as discussed above.
The residence time in this step is likewise not subject to any restrictions, but economic reasons generally dictate a range from about 10 minutes to about 10 hours, preferably from about 60 to about 8 hours, particularly preferably from about 60 minutes to about 6 hours.
The product mixture obtained in step 3 can be further processed as described below.
In a preferred embodiment, the product mixture of step 3 is subjected to a postcondensation in a fourth step at a temperature from about 200 to about 350°C,

preferably at a temperature from about 220 to 300°C, especially from about 250 to 270°C. Step 4 is carried out at a pressure which is below the pressure of step 3 and is preferably within the range from about 5 to 1000 x 103 Pa, more preferably within the range from about 10 to about 300 x 103 Pa. In the context of this step, the temperature and pressure are selected so as to obtain a second gas phase and a second liquid or solid phase or a mixture of second liquid and second solid phase which each comprise the polyamide.
The postcondensation of step 4 is preferably carried out in such a way that the relative viscosity (measured at a temperature of 25°C and a concentration of 1 g of polymer per 100 ml in 96% strength by weight of sulfuric acid) of the polyamide assumes a value within the range from about 1.6 to about 3.5.
In a preferred embodiment, any water present in the liquid phase can be expelled by means of an inert gas such as nitrogen.
The residence time of the reaction mixture in step 4 depends especially on the desired relative viscosity, the temperature, the pressure and the amount of water added in step
3.
If step 3 is operated as a single-phase regime, the product line between step 3 and step 4 may optionally contain packing elements, for example, Raschig rings or Sulzer mixing elements, which allow a controlled expansion of the synthesis mixture in the gas phase.
In a further embodiment of the invention, step 3 may be dispensed with and the polyamide produced by carrying out steps (1), (2) and (4).
This variant is preferably carried out as follows:

The reaction mixture is treated in step 2 as described above or at a temperature within the range from about 220 to about 300°C and a pressure within the range from about 1 to about 7x106 Pa, the pressure in the second step being at least 0.5 x 106 Pa lower than in step 1. At the same time, the resulting first gas phase is separated from the first liquid phase.
The first liquid phase obtained in step 2 is treated in step 3 as in step 1 or at a temperature within the range from about 220 to 300°C and a pressure within the range from about 10 to about 300 x 103 Pa, the resulting second, water- and ammonia-comprising gas phase being separated from the second liquid phase. Within this step, the relative viscosity (measured as defined above) of the resulting polyamide is adjusted to a desired value within the range from about 1.6 to about 3.5 through choice of temperature and residence time.
The resulting second liquid phase is then conventionally discharged and, if desired, worked up.
In a further preferred embodiment of the present invention, at least one of the gas phases obtained in the respective steps can be recycled into at least one of the preceding steps.
It is further preferable to select the temperature and pressure in step 1 or in step 3 or in both step 1 and step 3 so as to obtain a liquid or a solid phase or a mixture of liquid and solid phase and a gaseous phase and the gaseous phase is separated off.
Furthermore, in the context of the process of the invention, it is also possible to carry out a chain lengthening or branching or a combination thereof. For this purpose, polymer branching or chain-lengthening substances known to a person skilled in the

art are added in the individual steps. These substances are preferably added in step 3 or 4.
Usable substances are:
Trifunctional amines or carboxylic acids as branching agents or crosslinkers. Examples of suitable at least trifunctional amines or carboxylic acids are described in EP-A-0 345 648. The at least trifunctional amines have at least three amino groups which are capable of reaction with carboxylic acid groups. They preferably do not have any carboxylic acid groups. The at least trifunctional carboxylic acids have at least three carboxylic acid groups which are capable of reaction with amines and which can also be present, for example, in the form of their derivatives, such as esters. The carboxylic acids preferably do not contain any amino groups capable of reaction with carboxylic acid groups. Examples of suitable carboxylic acids are trimesic acid, trimerized fatty acids, which can be prepared for example from oleic acid and can have from 50 to 60 carbon atoms, naphthalenepolycarboxylic acids, such as naphthalene-1,3,5,7-tetracarboxylic acid. The carboxylic acids are preferably defined organic compounds and not polymeric compounds.
Examples of amines having at least 3 amino groups are nitrilotrialkylamine, especially nitrilotriethaneamine, dialkylenetriamines, especially diethylenetriamine, trialkylene-tetramines and tetraalkylenepentamines, the alkylene moieties preferably being ethylene moieties. Furthermore, dendrimers can be used as amines. Dendrimers preferably have the general formula I
(R2N-(CH2)n)2N-(CH2)x-N((CH2)n-NR2)2 (I)
where

R is H or -(CH2)n-NR12, where R1 is H or -(CH2)n-NR22, where R2 is H or -(CH2)n-NR32, where R3 is H or -(CH2)n-NH2, n is an integer from 2 to 6, and x is an integer from 2 to 14.
Preferably, n is 3 or 4, especially 3, and x is an integer from 2 to 6, preferably from 2 to 4, especially 2. The radicals R can also have the stated meanings independently of one another. Preferably, R is a hydrogen atom or a -(CH2)n-NH2 radical.
Suitable carboxylic acids are those having from 3 to 10 carboxylic acid groups, preferably 3 or 4 carboxylic acid groups. Preferred carboxylic acids are those having aromatic and/or heterocyclic nuclei. Examples are benzyl, naphthyl, anthracene, • biphenyl, triphenyl radicals or heterocycles such as pyridine, bipyridine, pyrrole, indole, furan, thiophene, purine, quinoline, phenanthrene, porphyrin, phthalocyanine, naphthalocyanine. Preference is given to 3,5,3",5"-biphenyltetracarboxylic acid- : phthalocyanine, naphthalocyanine, 3,5,5",5"-biphenyltetracarboxylic acid, 1,3,5,7-naphthalenetetracarboxylic acid, 2,4,6-pyridinetricarboxylic acid, 3,5,3",5"-bipyrid-yltetracarboxylic acid, 3,5,3",5"-benzophenonetetracarboxylic acid, 1,3,6,8-acridinetetracarboxylic acid, particularly preferably 1,3,5-benzenetricarboxylic acid (trimesic acid) and 1,2,4,5-benzenetetracarboxylic acid. Such compounds are commercially available or can be prepared by the process described in DE-A-43 12 182. If ortho-substituted aromatic compounds are used, imide formation is preferably prevented through the choice of suitable reaction temperatures.
These substances are at least trifunctional, preferably at least tetrafunctional. The number of functional groups can be from 3 to 16, preferably from 4 to 10, particularly preferably from 4 to 8. The processes of the invention are carried out using either at

least trifunctional amines or at least trifunctional carboxylic acids, but not mixtures of such amines or carboxylic acids. However, small amounts of at least trifiinctional amines may be present in the trifunctional carboxylic acids, and vice versa.
The substances are present in an amount from 1 to 50 mmol/g of polyamide, preferably from 1 to 35, particularly preferably 1 to 20, umol/g of polyamide. The substances are preferably present in an amount from 3 to 150, particularly preferably from 5 to 100, especially from 10 to 70, μmol of equivalents/g of polyamide. The equivalents are based on the number of functional amino groups or carboxylic acid groups.
Difunctional carboxylic acids or difunctional amines are used-as chain lengtheners. These have 2 carboxylic acid groups which can be reacted with amino groups, or 2 amino groups which can be reacted with carboxylic acids. The difunctional carboxylic acids or amines, as well as the carboxylic acid groups or amino groups, do not contain any further functional groups capable of reaction with amino groups or carboxylic acid groups. Preferably, they do not contain any further functional groups. Examples of suitable difunctional amines are those which form salts with difunctional carboxylic acids. They can be linear aliphatic, such as C1.14-alkylenediamine, preferably C2-6-alkylenediamine, for example hexylenediamine. They can also be cycloaliphatic. Examples are isophoronediamine, dicycycan, laromine. Branched aliphatic diamines are likewise usable, an example being Vestamin TMD (trimethylhexamethylenediamine, from Huls AG). In addition, the diamines can also be aromatic-aliphatic, it being possible to use n-xylylenediamine, for example. Entire amines can each be substituted by Ci-12-alkyl, preferably Ci-14-alkyl, radicals on the carbon skeleton.
- , t
Difunctional carboxylic acids are, for example, those which form salts with
difunctional diamines. They can be linear aliphatic dicarboxylic acids, which are
preferably C4-20-dicarboxylic acids. Examples are adipic acid, azelaic acid, sebacic

acid, suberic acid. They can also be aromatic. Examples are isophthalic acid, terephthalic acid, naphthalenedicarboxylic acid, as well as dimerized fatty acids.
The difunctional basic building blocks (c) are preferably used in amounts from 1 to 55, particularly preferably from 1 to 30, especially from 1 to 15, mm/g of polyamide.
According to the invention, the product mixture obtained in step 3, or the second liquid or second solid phase or the mixture of second liquid and second solid phase (from step 4) which each comprise the polyamide, preferably a polymer melt, is discharged from the reaction vessel in a conventional manner, for example by means of a pump. Subsequently, the polyamide obtained can be worked up according to conventional methods, as described for example in DE-A 43 21 683 (page 3 line 54 to page 4 line 3) at length.
In a preferred embodiment, the level of cyclic dimer in the nylon-6 obtained according to the invention can be further reduced by extracting the polyamide first with an aqueous solution of caprolactam and then with water and/or subjecting it to a gas phase extraction (described in EP-A-0 284 968, for example). The low molecular weight constituents obtained in this aftertreatment, such as caprolactam, linear caprolactam oligomer and cyclic caprolactam oligomer, can be recycled into the first and/or second and/or third step.
The starting mixture and the synthesis mixture can be admixed in all steps with chain regulators such as aliphatic and aromatic carboxylic and dicarboxylic acids and catalysts such as oxygen-containing phosphorus compounds in amounts within the range from 0.01 to 5% by weight, preferably within the range from 0.2 to 3% by weiglft, based on the amount of polyamide-forming monorrters and aminohitriles used. Suitable chain regulators include for example propionic acid, acetic acid, benzoic acid, terephthalic acid and triacetonediamine.

Additives and fillers such as pigments, dyes and stabilizers are generally added to the synthesis mixture prior to pelletization, preferably in the second, third and fourth steps. Particular preference is given to using fillers and additives whenever the synthesis or polymer mixture will not encounter fixed bed catalysts in the rest of the processing. One or more impact-modifying rubbers may be present in the compositions as additives in amounts from 0 to 40% by weight, preferably from 1 to 30% by weight, based on the entire composition.
It is possible to use, for example, customary impact modifiers which are suitable for polyamides and/or polyarylene ethers.
Rubbers which enhance the toughness of polyamides generally have two essential features: they have an elastomeric portion which has a glass transition temperature of less than -10°C, preferably less than -30°C, and they contain at least one functional group which is capable of interaction with the polyamide. Suitable functional groups include for example carboxylic acid, carboxylic anhydride, carboxylic ester, carboxylic amide, carboxylic imide, amino, hydroxyl, epoxide, urethane and oxazoline groups.
Examples of rubbers which enhance the toughness of the blends include for example:
EP and EPDM rubbers grafted with the above functional groups. Suitable grafting reagents include for example maleic anhydride, itaconic acid, acrylic acid, glycidyl acrylate and glycidyl methacrylate.
These, monomers can be grafted onto the polymer in the melt, or in solution, in the presence or absence of a free-radical initiator such as cumene hydroperoxide.

The copolymers of a-olefins described under the polymers A, including especially the ethylene copolymers, may also be used as rubbers instead of polymers A and be mixed as such into the compositions of the invention.
A further group of suitable elastomers are core-shell graft rubbers. These are graft rubbers which are produced in emulsion and which have at least one hard and one soft constituent. A hard constituent is customarily a polymer having a glass transition temperature of at least 25°C, while a soft constituent is a polymer having a glass transition temperature of not more than 0°C. These products have a structure made up of a core and at least one shell, the structure being the result of the order in which the monomers are added. The soft constituents are generally derived from butadiene, isoprene, alkyl acrylates, alkyl methacrylates or siloxanes and optionally further comonomers. Suitable siloxane cores can be prepared for example starting from cyclic oligomeric octamethyltetrasiloxane or tetravinyltetramethyltetrasiloxane. These can be, for example, reacted with y-mercaptopropylmethyldimethoxysilane in a ring-opening cationic polymerization, preferably in the presence of sulfonic acids, to form the soft siloxane cores. The siloxanes can also be crosslinked by, for example, conducting the polymerization reaction in the presence of silanes having hydrolyzable groups such as halogen or alkoxy groups such as tetraethoxysilane, methyltri-methoxysilane or phenyltrimethoxysilane. Suitable comonomers here include for example styrene, acrylonitrile and crosslinking or grafting monomers having more than one polymerizable double bond such as diallyl phthalate, divinylbenzene, butanediol diacrylate or triallyl (iso)cyanurate. The hard constituents are generally derived from styrene, a-methylstyrene and copolymers thereof, preferred comonomers being acrylonitrile, methacrylonitrile and methyl methacrylate.
Preferred core-shell graft rubbers have a soft core and a hard shell or a hard core, a first 30ft shell and at least one further hard shell. The incorporation of functional groups such as carbonyl, carboxylic acid, acid anhydride, acid amide, acid imide, carboxylic esters, amino, hydroxyl, epoxy, oxazoline, urethane, urea, lactam or halobenzyl groups is here preferably effected by the addition of suitably

functionalized monomers during the polymerization of the last shell. Suitable functionalized monomers include for example maleic acid, maleic anhydride, mono-or diesters or maleic acid, tert-butyl (meth)acrylate, acrylic acid, glycidyl (meth)acrylate and vinyloxazoline. The proportion of monomers having functional groups is generally within the range from 0.1 to 25% by weight, preferably within the range from 0.25 to 15% by weight, based on the total weight of the core-shell graft rubber. The weight ratio of soft to hard constituents is generally within the range from 1:9 to 9:1, preferably within the range from 3:7 to 8:2.
Such rubbers, which enhance the toughness of polyamides, are known per se and described in EP-A-0 208 187, for example.
A further group of suitable impact modifiers are thermoplastic polyester elastomers. Polyester elastomers are segmented copolyetheresters containing long-chain segments, generally derived from poly(alkylene) ether glycols, and short-chain segments, derived from low molecular weight diols and dicarboxylic acids. Such products are known per se and are described in the literature, for example in US 3,651,014. Corresponding products are also commercially available under the names of Hytrel® (Du Pont), Arnitel® (Akzo) and Pelprene® (Toyobo Co. Ltd.).
It will be appreciated that it is also possible to use mixtures of different rubbers.
As further additives there may be mentioned for example processing aids, stabilizers and oxidation retardants, agents against thermal decomposition and decomposition by ultraviolet light, lubricating and demolding agents, flame retardants, dyes and pigments and plasticizers. The proportion thereof is generally up to 40%, preferably up to 15%o, by weight, based on the total weight of the composition.
Pigments and dyes are generally present in amounts of up to 4%, preferably from 0.5 to 3.5%o, especially from 0.5 to 3%, by weight.

The pigments for coloring thermoplastics are commonly known, see for example R. Gachter and H. Muller, Taschenbuch der Kunststoffadditive, Carl Hanser Verlag, 1983, pages 494 to 510. The first preferred group of pigments to be mentioned are white pigments such as zinc oxide, zinc sulfide, lead white (2 PbC03 • Pb(OH)2), lithopone, antimony white and titanium dioxide. Of the two most common crystal polymorphs (rutile and anatase) of titanium dioxide, the rutile form is preferred for use as white pigment for the molding compositions of the invention.
Black pigments which can be used according to the invention are iron oxide black (Fe3O4), spinel black (Cu(Cr,Fe)2O4), manganese black (mixture of manganese dioxide, silicon dioxide and iron oxide), cobalt black and antimony black and also, particularly preferably, carbon black, which is usually used in the form of furnace or gas black (see G. Benzing, Pigmente fur Anstrichmittel, Expert-Verlag (1988), p. 78ff).
It will be appreciated that inorganic color pigments such as chromium oxide green or organic color pigments such as azo pigments and phthalocyanines can be used according to the invention to obtain certain hues. Such pigments are generally commercially available.
It can further be of advantage to use the abovementioned pigments or dyes in a mixture, for example carbon black with copper phthalocyanines, since this generally facilitates the dispersion of color in the thermoplastic.
Oxidation retardants and thermal stabilizers which can be added to the thermoplastic compositions of the invention include for example halides of metals of group I of the periodic table, e.g., sodium halides, potassium halides, lithium halides, optionally in conjunction with copper(I) halides, for example chlorides, bromides 6r iodides. The halides, especially of copper, may also contain electron-rich p-ligands. Examples of

such copper complexes are copper halide complexes with triphenylphosphine, for example. It is further possible to use zinc fluoride and zinc chloride. Other possibilities are sterically hindered phenols, hydroquinones, substituted represen¬tatives of this group, secondary aromatic amines, optionally in conjunction with phosphorus-containing acids and salts thereof, and mixtures of these compounds, preferably in a concentration up to 1% by weight, based on the weight of the mixture.
Examples of UV stabilizers are various substituted resorcinols, salicylates, benzo-triazoles and benzophenones, which are generally used in amounts of up to 2% by weight.
Lubricating and demolding agents, which are generally included in the thermoplastic material in amounts of up to 1% by weight, are stearic acid, stearyl alcohol, alkyl stearates and N-alkylstearamides and also esters of pentaerythritol with long-chain fatty acids. It is also possible to use salts of calcium, of zinc or of aluminum of stearic acid and also dialkyl ketones, for example distearyl ketone.
The present invention further provides a polyamide producible by any of the foregoing processes.
The examples which follow illustrate the invention.

Examples
Measurement of residence time distribution
The effect of the various mixing elements on the residence time distribution is investigated in a glass tubular reactor. The glass cylinder, which has the same length (100 cm) and the same internal diameter (3.6 cm) as the tubular reactor used for ACN direct polymerization, is fitted with the corresponding mixing elements for this purpose. The mixing elements used are 3 mm Raschig rings or TiO2 extrudates (diameter 4 mm, length 5-10 mm). Water is pumped through the flow tube at a rate of 600 g/h using an HPLC pump.
Methylene blue (0.05% strength) is used as tracer. The tracer solution is fed to the reactor inlet, again at a rate of 600 g/h, via the main feed line. During the injection of the tracer solution, which takes 1 minute, the feed of the tracer-free liquid is interrupted. Samples are taken at the reactor outlet at intervals within the range from 3 to 5 minutes. The tracer concentration of the samples is determined via absorption spectroscopy.
Characterization of the residence time distribution through calculation of the Bodenstein number
The purpose of the analysis is to characterize the measured residence time distributions, so that the effect of the mixing elements can be compared. The average residence time t" and the Bodenstein number Bo, which is a measure of the width, and shape of distribution time curves, are suitable t parameters here for demonstrating the dependence of the residence time behavior on the mixing element.

The measured concentration (T) - time profiles (Z) (T in arbitrary units, Z in minutes) of the tracers display distinct departures from a Gaussian distribution, evidence of pronounced axial dispersion. It therefore appears sensible to employ the dispersion model for real reactors, which is described for example in Octave Levenspiel, Chemical Engineering, 2nd Edition, John Wiley & Sons, New York (1962), for describing the response function means measured. This model introduces a diffuse term with the dispersion coefficient D which takes account of the degree of axial mixing. The analytic solution of the dispersion model describes the dependence of the response function C on the dimensionless quotient Bo, the Bodenstein number.

where u is the hydrodynamic flow velocity, L is the path length, D is the dispersion coefficient and D is the hydrodynamic residence time. The shape of the residence time curves depends on the axial dispersion and is thus a function of the Bodenstein number. The larger the Bodenstein number, the more the flow in the reactor corresponds to an ideal plug flow. By fitting equation (1) to the normalized response functions, the appropriate values are obtained for the (fitting) parameters Bo and T.

Catalyst preparation
Catalyst 1 Beta-zeolite powder
The catalyst used was a beta-zeolite from Uetikon (Zeokat-Beta) having the following composition: Si02 = 91%, A1203 = 7.8%, Na20 = 0.5%, K20 = 0.7%, BET surface area = 700 m2/g, pore size in A = 7.6 x 6.7; 5.5 x 5.5, particle size 0.2-0.5 mm.
Catalyst 2 Beta-zeolite extrudates
220 g of P-zeolite from Example 1 were kneaded with 5% of Walocel® and 230 g of water for 45 minutes. The material was then molded under a pressure of 70 bar into 2 mm extrudates. These were dried at 110°C and calcined at 500°C for 16 h.
195 g of these extrudates were exchanged with 3 liters of 20%> strength NH4CI solution at 80°C for 2 h and then washed with 10 1 of water. Thereafter a second exchange was effected again with 3 1 of 20%) strength NH4CI solution at 80°C/2 h and the product was washed Cl-free. Drying at 110°C was followed by 5 h of calcination at 500°C.
Catalyst 3 Sheet-silicate type K10®
K10® is an acid-treated montmorillonite from Sud-Chemie. It has a BET surface area of 180-220 m7g and an ion exchange equivalent of 40-50 meq/100 g.

Catalysts 4 and 5 TiCh extrudates of 100% and 84% anatase, respectively
Preparation is in line with the description in Ertl, Knozinger, Weitkamp: "Handbook of heterogeneous catalysis", VCH Weinheim, 1997; page 98ff. The T1O2 polymorphs described as particularly preferred in the preceding description were mixed with water, silica sol and glycerol, extruded and calcined at 550°C.
Catalyst 6 Titanium dioxide/tungsten oxide catalyst
The catalyst used was obtained by intimately mixing the commercially available titanium dioxide VKR 611 (from Sachtleben) with tungsten oxide and subsequent extrusion as per Example 2 or 4.
It has the following specification: 20% by weight of WO3, 80% by weight of TiO?; BET surface area = 73 m2/g, total acidity (pKa = 6.8) = 0.56 mmol/g; total acidity (pKa=-3) = 0.035mmol/g.
Inventive Examples 1-3
The table shows the improvement in the residence time distribution, i.e., the reduction in axial backmixing, obtained through the use of TiO2 pellets (catalyst 4: extrudates 4 mm in thickness and about 7 mm in average length). Compared with the pure TiO2 bed (Comparative Example CI) and the T1O2 free bed of the Raschig ring packing elements (Comparative Example C2), the residence time distribution of Inventive Examples 1 and 2 is narrower, i.e., the Bodenstein number Bo is larger.

The result measured for Inventive Example 1, in which T1O2 pellets and Raschig rings are used as packing elements in the reactor, and of Comparative Example C2 with (exclusively) Raschig rings is depicted in Figure 1 together with the calculated residence time curves.
The alternating beds in the tubular reactor are characterized by the layer thickness and the packing elements used. The stated order of the beds corresponds to the bed sequence in the reactor in the direction of flow, i.e., in the upward direction.

We claim:
1. A continuous process for producing a polyamide by reacting at least one aminonitrile with water, comprising the following steps:
(1) reacting at least one aminonitrile with water in a molar ratio of from 1:1 to 1:10 at a temperature from 90 to 400°C and a pressure from 0.1 to 15 x 106 Pa in a flow tube containing packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements and metallic packing elements wherein the packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements and the metallic packing elements form alternating layers in the flow tube, to obtain a reaction mixture,
(2) further reacting the reaction mixture at from 150 to 400°C and a pressure which is lower than the pressure in step 1, the temperature and pressure being selected so as to obtain a first gas phase and a first liquid or a first solid phase or a mixture of first solid and first liquid phase, and the first gas phase is separated from the first liquid or first solid phase or the mixture of first liquid and first solid phase, and
(3) admixing the first liquid or the first solid phase or the mixture of first liquid and first solid phase with a gaseous or liquid phase comprising water at a temperature from 150 to 370°C and a pressure from 0.1 to 30 x 10 Pa to obtain a product mixture.

2. The process as claimed in claim 1, wherein step (3) is performed in a flow tube containing packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements and metallic packings wherein the packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements and the metallic packing elements form alternating layers in the flow tube.
3. The process as claimed in claim 1 or 2, further comprising the following step: postcondensing the product mixture at a temperature from 200 to 350°C and a pressure which is lower than the pressure in step 3, the temperature and pressure being selected so as to obtain a second, water- and ammonia-comprising gas phase and a second liquid or second solid phase or a mixture of second liquid and second solid phase, which each comprise the polyamide.
4. The continuous process for producing a polyamide by reacting at least one aminonitrile with water, comprising the steps of reacting at least one aminonitrile with water in a molar ratio of from 1:1 to 1:10 at a temperature from 90 to 400°C and a pressure from 0.1 to 15 x 106 Pa in a flow tube containing packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements and metallic packing elements wherein the packing elements of a Bronsted acid catalyst selected from beta-zeolite, sheet-silicate or titanium dioxide packing elements and the metallic packing elements form alternating layers in the flow tube, to obtain a reaction mixture, further reacting the reaction mixture at from 150 to 400°C and a pressure which is lower than the pressure in step 1, the temperature and pressure being selected so as to obtain a first gas phase and a first liquid or a first solid phase or a mixture of first solid and first liquid phase, and the first gas phase is separated from the first liquid or first solid phase or the mixture of first liquid and first solid phase, and postcondensing the first

liquid or the first solid phase or the mixture of first liquid and first solid phase at a temperature from 200 to 350°C and a pressure which is lower than the pressure in step 2, the temperature and pressure being selected so as to obtain a second, water- and ammonia-comprising gas phase and a second liquid or second solid phase or a mixture of second liquid and second solid phase, which each comprise the polyamide.
5. The process as claimed in any of claims 1 to 4, wherein the temperature and pressure in step 1 or in step 3 or both in step 1 and step 3 are selected so as to obtain a liquid or a solid phase or a mixture of liquid and solid phase and a gaseous phase and the gaseous phase is separated off.
6. The process as claimed in any of claims 1 to 5, wherein the titanium dioxide packing elements consist of Ti02 comprising from 70 to 100% by weight of anatase and from 0 to 30% by weight of rutile and in which up to 40% by weight of the titanium dioxide may be replaced by tungsten oxide.
7. The process as claimed in any of claims 1 to 6, wherein at least one of the gas phases obtained in the respective steps is recycled into at least one of the preceding steps.
8. The process as claimed in any of claims 1 to 7, wherein the aminonitrile reacted is an α -aminoalkyl nitrile having an alkylene moiety (-CH2-) of from 4 to 12 carbon atoms or an aminoalkylaryl nitrile having from 8 to 13 carbon atoms.

9. The process as claimed in any of claims 1 to 8 for the preparation of
copolyamides, branched or chain lengthened polyamide a mixture consisting
of:
from 50 to 99.99% by weight of 6-aminocapronitrile,
from 0.01 to 50% by weight of at least one dicarboxylic acid selected from the
group consisting of aliphatic C4-Cio-a,G)-di-carboxylic acids, aromatic C8-Ci2-
dicarboxylic acids and C5-Q-cycloalkanedicarboxylic acids,
from 0 to 50% by weight of an a,co-diamine having 4-10 carbon atoms,
from 0 to 50% by weight of an a,co-C2-Ci2-dinitrile,
from 0 to 50% by weight of an aα -C5-C12-amino acid or of the corresponding
lactam, and
from 0 to 10% by weight of at least one inorganic acid or salt thereof, the
individual weight percentages adding up to 100% is reacted.
10. A continuous process for producing a polyamide substantially as herein
described with reference to the accompanying drawings.

Documents:

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in-pct-2000-0215-che-form-3.pdf

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Patent Number

214486

Indian Patent Application Number

IN/PCT/2000/215/CHE

PG Journal Number

13/2008

Publication Date

31-Mar-2008

Grant Date

12-Feb-2008

Date of Filing

26-Jul-2000

Name of Patentee

BASF AKTIENGESELLSCHAFT

Applicant Address

67056 Ludwigshafen,

Inventors:

#	Inventor's Name	Inventor's Address
1	Ralf MOHRSCHLADT	Sternallee 5, D-68723 Schwetzingen,
2	Dieter KRAUSS	Langgasse 38, D-67269 Grunstadt,
3	Volker HILDEBRANDT	Am Brunnengarten 23, D-68169 Mannheim,

PCT International Classification Number

C08G 69/04

PCT International Application Number

PCT/EP99/00602

PCT International Filing date

1999-01-29

PCT Conventions:

#	PCT Application Number	Date of Convention	Priority Country
1	198 04 033.4	1998-02-02	Germany