Title of Invention	A DEVICE FOR PRODUCING UREA
Abstract	A device for producing urea The present invention relates to a device for producing urea by reacting a liquid phase including ammonia and a gas phase including carbon dioxide separating the liquid phase from the gas phase by means of a plurality of plates. The liquid steps flows through a plurality of first openings in at least one of the plates. The gas phase flows through the second openings of the plates. The liquid phase and the gas phase are distributed through the reactor in a even, continuous and permanent flow.

Title of Invention

A DEVICE FOR PRODUCING UREA

Abstract

A device for producing urea The present invention relates to a device for producing urea by reacting a liquid phase including ammonia and a gas phase including carbon dioxide separating the liquid phase from the gas phase by means of a plurality of plates. The liquid steps flows through a plurality of first openings in at least one of the plates. The gas phase flows through the second openings of the plates. The liquid phase and the gas phase are distributed through the reactor in a even, continuous and permanent flow.

Full Text	This invention relates to a device for producing urea. The present invention concerns device for increasing the yield while at the same time increasing the production potential of reactors for producing urea, formed by synthesis between ammonia and carbon dioxide at high pressure and temperature. The reactors include an internal space for cocurrent fluid flow by a liquid phase and a gas phase, the internal space being divided into compartments to avoid excessive mixing of the liquid phase and to allow for intermittent redistribution of gas in bubbles of a size suitable for increasing heat and matter exchange between the two phases. The device of the present invention consists substantially of seven perforated flat plates distributed transversely in a cylindric reactor shell for creating compartments therein, through which flow gas and liquid containing urea. In modern reactors for the synthesis of urea, two phase ,a gas phase and a liquid phase, flow cocurrently inside the cylindrical shell of the reactor (which is under pressure). The shell is divided into compartments by seven perforated plates. The purpose of this configuration is to avoid excessive mixing of the entire liquid phase contained in the reactor, which would tend to turn it into a complete mixing reactor, thus reducing the urea yield. The amount of mixing is reduced by dividing the reactor into several stages by means of seven plates. The behavior of the liquid phase approaches that of the behavior of a piston flow reactor, which is notoriously the most favorable for keeping the urea yield relatively high. By dividing the reactor into seven stages by means of perforated plates, it is also possible to redistribute the gas which flows upwards along the column intermittently in smaller bubbles more suitable for increasing heat and matter exchange between the two phases. In effect, the rising showers of bubbles are subjected to coalescence phenomena which progressively increase the size of the bubbles, thus reducing the exchange surface between phases. This negative phenomena is partly compensated for by the redistribution brought about by the perforated flat plates. However, the cocurrent flow of gas and liquid over each perforated plate produces some adverse effects on both the heat and matter exchange and the urea yield (the latter is due to a diminution of the flow of reagents into the liquid phase, as well as to the reduction in temperature because of the smaller exothermic reaction and also to the reduction in the liquid hold-up in the reactor). In effect, steam and liquid cannot go through the perforations in the flat baffles simultaneously, but are forced to do so alternately by means of forming showers of steam bubbles, separated by liquid pistons in continuous phase. Such an arrangement, as compared with a uniform distribution of the bubbles, with the same amount of steam brings about a higher concentration of bubbles inside the showers alternating with the liquid pistons. The result is a significant increase in coalescence of the bubbles between one plate and the next (increasing their average size), a reduction of the steam/liquid surface, and a worsening of the gas phase/liquid phase exchange since less steam is exchanged with the liquid phase. The volume available for this phase is also reduced (and the temperature it has reached is also lowered). Moreover, between the plates and the cylinder there is in general a circular slit through which part of the steam may go with less exchange efficiency. All this causes a reduction of the urea yield, compared with the yield obtainable with a uniform distribution, instead of the alternating one, of the gas bubbles after each perforated plate. Another limitative aspect of the state of the art concerns the possibility of increasing the production potential in reactors in existing plants is limited. Generally, the reactor, due to its potential liquid phase capacity, is very large compared to the nominal urea production required of it, and this fact would lend itself, in principle, to possible increases in production with an almost constant urea yield. However, urea yield drastically worsens as the gas and liquid capacity increases, because of the poor distribution of gas, the size of the bubbles due to parasitical coalescence, the matter and heat exchange between phases, the effective volume left to the liquid phase (in which the reaction forming the urea takes place). Accordingly, urea production does not increase proportionately to the increase in total liquid and gas capacity. The main purpose of this invention is to provide a device to eliminate the above-mentioned drawbacks and to increase the synthesis reaction yield and the potential of urea reactors. Another purpose of the invention is to provide particularly simple and efficient devices to put into effect the method. In every transfer from one compartment into the other the gas and liquid phases are made to flow in mutually separate and distributed ways, each with a continuous, permanent and even flow. In a preferred embodiment, the working device is characterized by the fact that the perforations in plates having dimensional and/or shape gradients which create area fractions which permit the flow of liquid in the substantial absence of gas bubbles. The bubbles sliding and being evenly distributed and concentrated in an area which would be hard to reach by the liquid. Therefore, according to an aspect of this invention, the reactor"s perforated plates are made in such a way as to allow the more even distribution, with a permanent flow, of the gas bubbles avoiding their coalescing between plates and the adverse effects of the two-phase movement discussed above with showers of bubbles alternating with a continuous liquid flow. The result is an increase in urea yield and of the reactor"s production potential. In a particularly simple and efficient and therefore preferred embodiment, the plates are differently perforated and shaped in such a way as to allow the continuous and permanent flow of both the gas and the liquid, both flowing along routes which are mutually separate and distributed through each plate. The size of the perforations is different for the area of the plate for the flow of liquid and the flow of gas. The size of the perforations in the areas intended for the flow of liquid being such as to impede the passage through them of gas bubbles together with the liquid, but rather to favor sliding of the bubbles toward zones intended for the gas flow. The area for the flow of the two phases are distributed in such a way as to ensure the even distribution of the gas bubbles through said shaped perforated plates. Accordingly the present invention relates to a device for producing urea, comprising a plurality of plates (SP1 -SP3) insertable within the internal space of a reactor (R) for producing urea, wherein at least one of said plates (SP1 -SP3) comprises: a plurality of first openings (Fi) having a first predetermined size suitable for flowing predominantly the liquid phase therethrough; and a plurality of second openings (fi) having a second predetermined size suitable for flowing predominantly the gas phase therethrough; the first openings (Fi) favoring flow therethrough of the liquid phase substantially free of gas bubbles and the second openings (fi) favoring flow therethrough of the gas phase substantially free of the liquid phase, whereby each of the liquid phase and the gas phase are distributed through the reactor (R) in a substantially even, continuous and permanent flow. The various aspects and advantages of the invention will be made more clear by the description of the embodiment represent in the accompanying drawings in which; Fig. 1 shows the schematic and partial longitudinal section of a multi¬compartment reactor. Fig. 2 is an enlarged scale view of the elements forming the plates, comprised in circle A in fig. 1; Fig 3 is an overhand view of the upper part 2 of an element ELi; Fig. 3 A shows the section along the line A-A of a rectangular ELi element; Fig. 4 is the front view of a plate SPi formed by rectangular element EL" i-EL"n; Fig. 4A (analogous to fig. 2) is an enlarged view of elements EL" m-1, EL" m, EL"m+1 in fig. 4; Figs. 5 and 5 A are enlarged views of perforated portions on wall 2 (at right angles to the reactor"s axis) respectively on walls 4, 4" parallel with the axis. In fig. 1, R shows the central cylindrical shell of the urea reactor and CI, C2, C3 are the three transversal compartments created by the three plates SP1, SP2 and SP3. Atleast one of these plates comprises a plurality of upwardly extending element (ELI-Elm). These upwardly extending elements are preferably lozenge shaped elements ELI ELn which in fig. 2 are trapeze-shaped and which in fig. 4 are rectangular by preference. Fig. 2 shows that every ELi element is shaped like a Greek key, with a wall shaped like an upside down trapeze formed by the side or lesser base 2 at the top, by the greater base at the bottom 3, by the two slanting sides 4 and 4", and by airspace 5. According to the main aspect of the invention, in the embodiment shown in FIG. 2, on the two slanting sides 4 and 4" there are perforations Fi larger than perforations fi on wall 2. Preferably, perforations fi have a diameter which is between 1 and 3.5 mm, most preferably, about 2 to 3 mm, while the large perforations Fi have a diameter which is almost twice that of fi, i.e., 2 to 7 mm, perforations Fi being preferably 3 to 6 mm. FIG. 3 shows a top view of a wall 2 of a rectangular or trapeze-shaped element EL"i. FIG. 4 shows the front view of a flat plate, perforated and formed by elements from EL"I to EL"n which are rectangular, i.e., with walls 4 and 4" parallel with the reactor"s axis. Perforations fi on wall 2 are generally circular as in FIG. 5. On the other hand, perforations Fi on walls 4 and 4" may be substantially ellipse-shaped as shown in FIG. 5A as O. They are characterized by a greater axis AM and by a smaller axis MI. EXAMPLE Operations have been carried out by simulation on a reactor whose model has supplied, under nominal design conditions, for a production of about 1800 t/d, a yield of 64% on the total flow (liquid plus gas). If the yield were to be (improperly) estimated on the sole liquid phase, it would be about 65.5%. By increasing production up to about 2300 t/d, a diminution in yield was noticed. This confirms, indirectly, a) that the reactor is far too big, b) that an improvement in transport processes inside the reactor would not only increase the yield, compared to nominal conditions, but would also improve yield which would be maintained throughout notable increases of its potential. Operations were then continued by simulating with a rigorous mathematical model conditions for a daily production of 23001. in the unmodified reactor. A yield (simulated) was obtained of 61.3%, which, if based (improperly) on the sole liquid phase would yield 63.5%. The absence of a number of data under these conditions does not allow for immediate confirmation, but it would seem that the effective yield predicted by the model under increased production conditions is reasonably close to reality. Simulation (through the model) of introducing into the reactor new plates in the 16 meters of the lower tangential line of the reactor was then carried out. The model modified in accordance with the invention has shown (for the potential of 2300 t/d already achieved) a yield of 65.8% (+4.5%) absolute) in respect of the total flow (equal to, improperly, 66.7% on the liquid phase, but with a drastic reduction in steam). It has also been confirmed that such yield can be maintained for further increases in potential up to 2700 t/d (if that were made possible by the other equipment in the plant). This is a further advantage of the invention. Consequently, in theory, under the conditions taken into consideration, an increase in yield (simulated) of 4.5% absolute could be obtained and further increases in production would be tolerable. Some elements resulting from experiments are given below. In the description, which follows, linear dimensions for baffles and for the passage of liquids are indicative. If necessary for construction purposes, they can be varied by about 5\|jl0%. This also applies to the number of perforations per meter both where the liquid phase and the gas phase passes. On the other hand, the size of the perforations for the gas phase must be considered unchangeable while those for the liquid phase are virtually so. Finally, it is confirmed that the number of perforations per square for the gas phase and the liquid phase should be read as referred to the areas for the gas phase and the liquid phase and not to the total area (gas plus liquid). Numbering of the plates (suggested, or actually existing, for that part which has not been replaced) begins at the lower tangential line (T.L.) of the reactor (not shown on drawings). In the same way, when the plates are being installed they should be rotated alternately (in respect of the dome directrix) by 60°-90° insofar as fastening points allow. It has been found that, on the whole, the following instructions should be followed when making the plates: -the thickness of the metal should not be more than 3.5-4 mm, to permit punching of the perforations; -the plates should be oriented alternately, for example, fixing them at right angles or at 60 °; -perforations for the installation should be made on that portion of the sheet metal reserved for the passage of liquid; -perforations per square meter for the surface intended for the passage of gas should be understood as referring to the entire surface of the sheet metal, even that which after being folded becomes lateral (vertical); -perforations for the gas should be made in equilateral triangular links with a 24 mm pitch; -after the plate has been shaped it is essential that the plates are closed at the ends with vertical walls welded to the terminal sections creating a seal to avoid gas escaping from the sides; -to make up for the thinness suitable supports or stiffeners can be applied to the sheet metal after perforating and shaping; -the gas should be introduced into the lower part through a horizontal tube with multiple perforations set at right angles to the lowest plate: if this were not possible, it would become necessary to arrange two plates, close to one another (300-500 mm) which would obtain the same result (since the lower plate would act as a distributor for the upper plate). The plates should be at a distance of about 2.4 m. Perforations for the gas could, in principle, be varied from one plate to the other, with a perforated area decreasing from bottom towards the top; however, with the plates arranged according to the invention, it is possible to maintain even perforations equal to the maximum perforations required for the lower plate. This simplifies construction and installation procedures. In the upper plates, the vapors (gas) are gradually decreasing, resulting in an increase of the level of the liquids inside the domes and a decrease of the head of gas (part of the perforations for the passage of gas will therefore be used by the liquid). In a preferred embodiment: -perforations for the gas (in the present case) were 2000 holes/(square meter of relative area) with a diameter 0=3 mm; arranged as an equilateral triangle (preferred arrangement), this means a distance between perforations, for example, of 24 mm (and a fraction of perforated area, on the area intended for gas, of 1.4%) (FIG. 5); perforations for the liquid (in the present case), 600 holes/(square meter of relative area) with diameter 08 mm, arranged as an equilateral triangle with a distance of 43 mm. Where oval perforations are used (FIG. 5A), their axes are 4 mm-6 mm, interspersed in the same way (with a fraction of perforated area of about 3% of the area for the liquid). Obviously, the metallic strips bearing the perforations, after being folded and installed, should be bolted one to another, leaving an edge for the alternating overlap from one dome to the next. For the sake of clarity and illustrative simplicity, the invention has been described with reference to the embodiments shown in the drawings. These however are subject to all those variations, substitutions, and modifications, etc. which being available to the average technician in this field can be considered as falling naturally within the wider scope and spirit of the invention. The Indian Patent 183121 (24/MAS/92) relates to reactor and a method for producing urea by reacting a liquid phase including ammonia and a gas phase including carbon dioxide separating the liquid phase for the gas phase by means of a plurality of plates. WE CLAIM: 1. A device for producing urea, comprising a plurality of plates (SP1 -SP3) insertable within the internal space of a reactor (R) for producing urea, wherein at least one of said plates (SP1 -SP3) comprises: a plurality of first openings (Fi) having a first predetermined size suitable for flowing predominantly the liquid phase therethrough; and a plurality of second openings (fi) having a second predetermined size suitable for flowing predominantly the gas phase therethrough; the first openings (Fi) favoring flow therethrough of the liquid phase substantially free of gas bubbles and the second openings (fi) favoring flow therethrough of the gas phase substantially free of the liquid phase, whereby each of the liquid phase and the gas phase are distributed through the reactor (R) in a substantially even, continuous and permanent flow. 2. The device according to claim 1, wherein at least one of said plates (SP1 -SP3) comprises a plurality of upwardly extending elements (ELI -ELn), said at least one plates (SP1 -SP3) being open at the bottom, and each said element (ELI - ELn) comprises: two perforated side walls (4, 4") defining a first area containing said first openings (Fi) of predetermined size for flow of the liquid phase substantially free of gas bubbles, and a perforated top wall (2) defining a second area containing said second openings (fi) having a second predetermined size for flow of the gas phase substantially free of the liquid phase. 3. The device according to claim 2, wherein said second openings (fi) in the top wall (2) are smaller in size than the first openings (Fi) in the side walls (4, 4"). 4. The device according to claim 2, wherein at least one of said plates (SP1 -SP3) comprises a plurality of elements (Ell -ELn) having rectangular cross-sections. 5. The device according to claim 2, wherein at least one of said plates (SP1 -SP3) comprises a plurality of elements (ELI -ELn) having trapezoidal cross-sections. 6. The device according to claim 2, wherein the first openings (Fi) in the side walls (4, 4") have a diameter of 2 to 7 mm and the second openings (fi) in the top wall (2) have a diameter of 1 to 3.5 mm. 7. The device according to claim 6, wherein the first openings (Fi) in the side walls (4, 4") have a diameter of from 3 to 6 mm and the second openings (fi) in the top wall (2) have a diameter of from 2 to 3 mm. 8. The device according to claim 2, wherein the first openings (Fi) in the side walls (4, 4") are elliptical. 9. The device according to claim 2, wherein the second openings (fi) in the top wall (2) are round. 10. A device for producing urea, substantially as hereinabove described and illustrated with reference to the accompanying drawings.

Full Text

This invention relates to a device for producing urea. The present invention concerns device for increasing the yield while at the same time increasing the production potential of reactors for producing urea, formed by synthesis between ammonia and carbon dioxide at high pressure and temperature. The reactors include an internal space for cocurrent fluid flow by a liquid phase and a gas phase, the internal space being divided into compartments to avoid excessive mixing of the liquid phase and to allow for intermittent redistribution of gas in bubbles of a size suitable for increasing heat and matter exchange between the two phases.
The device of the present invention consists substantially of seven perforated flat plates distributed transversely in a cylindric reactor shell for creating compartments therein, through which flow gas and liquid containing urea.
In modern reactors for the synthesis of urea, two phase ,a gas phase and a liquid phase, flow cocurrently inside the cylindrical shell of the reactor (which is under pressure). The shell is divided into compartments by seven perforated plates. The purpose of this configuration is to avoid excessive mixing of the entire liquid phase contained in the reactor, which would tend to turn it into a complete mixing reactor, thus reducing the urea yield. The amount of mixing is reduced by dividing the reactor into several stages by means of seven plates. The behavior of the liquid phase approaches that of the behavior of a piston flow reactor, which is notoriously the most favorable for keeping the urea yield relatively high.

By dividing the reactor into seven stages by means of perforated plates, it is also possible to redistribute the gas which flows upwards along the column intermittently in smaller bubbles more suitable for increasing heat and matter exchange between the two phases. In effect, the rising showers of bubbles are subjected to coalescence phenomena which progressively increase the size of the bubbles, thus reducing the exchange surface between phases. This negative phenomena is partly compensated for by the redistribution brought about by the perforated flat plates.
However, the cocurrent flow of gas and liquid over each perforated plate produces some adverse effects on both the heat and matter exchange and the urea yield (the latter is due to a diminution of the flow of reagents into the liquid phase, as well as to the reduction in temperature because of the smaller exothermic reaction and also to the reduction in the liquid hold-up in the reactor). In effect, steam and liquid cannot go through the perforations in the flat baffles simultaneously, but are forced to do so alternately by means of forming showers of steam bubbles, separated by liquid pistons in continuous phase. Such an arrangement, as compared with a uniform distribution of the bubbles, with the same amount of steam brings about a higher concentration of bubbles inside the showers alternating with the liquid pistons. The result is a significant increase in coalescence of the bubbles between one plate and the next (increasing their average size), a reduction of the steam/liquid surface, and a worsening of the gas phase/liquid phase exchange since less steam is exchanged with the liquid phase. The volume available for this phase is also reduced (and the temperature it has reached is also lowered). Moreover, between the plates and the cylinder there is in general a circular slit through which part of the

steam may go with less exchange efficiency. All this causes a reduction of the urea yield, compared with the yield obtainable with a uniform distribution, instead of the alternating one, of the gas bubbles after each perforated plate.
Another limitative aspect of the state of the art concerns the possibility of increasing the production potential in reactors in existing plants is limited. Generally, the reactor, due to its potential liquid phase capacity, is very large compared to the nominal urea production required of it, and this fact would lend itself, in principle, to possible increases in production with an almost constant urea yield. However, urea yield drastically worsens as the gas and liquid capacity increases, because of the poor distribution of gas, the size of the bubbles due to parasitical coalescence, the matter and heat exchange between phases, the effective volume left to the liquid phase (in which the reaction forming the urea takes place). Accordingly, urea production does not increase proportionately to the increase in total liquid and gas capacity.
The main purpose of this invention is to provide a device to eliminate the above-mentioned drawbacks and to increase the synthesis reaction yield and the potential of urea reactors.
Another purpose of the invention is to provide particularly simple and efficient devices to put into effect the method. In every transfer from one compartment into the other the gas and liquid phases are made to flow in mutually separate and distributed ways, each with a continuous, permanent and even flow.

In a preferred embodiment, the working device is characterized by the fact that the perforations in plates having dimensional and/or shape gradients which create area fractions which permit the flow of liquid in the substantial absence of gas bubbles. The bubbles sliding and being evenly distributed and concentrated in an area which would be hard to reach by the liquid.
Therefore, according to an aspect of this invention, the reactor"s perforated plates are made in such a way as to allow the more even distribution, with a permanent flow, of the gas bubbles avoiding their coalescing between plates and the adverse effects of the two-phase movement discussed above with showers of bubbles alternating with a continuous liquid flow. The result is an increase in urea yield and of the reactor"s production potential.
In a particularly simple and efficient and therefore preferred embodiment, the plates are differently perforated and shaped in such a way as to allow the continuous and permanent flow of both the gas and the liquid, both flowing along routes which are mutually separate and distributed through each plate. The size of the perforations is different for the area of the plate for the flow of liquid and the flow of gas. The size of the perforations in the areas intended for the flow of liquid being such as to impede the passage through them of gas bubbles together with the liquid, but rather to favor sliding of the bubbles toward zones intended for the gas flow. The area for the flow of the two phases are distributed in such a way as to ensure the even distribution of the gas bubbles through said shaped perforated plates.
Accordingly the present invention relates to a device for producing urea, comprising a plurality of plates (SP1 -SP3) insertable within the internal

space of a reactor (R) for producing urea, wherein at least one of said plates (SP1 -SP3) comprises: a plurality of first openings (Fi) having a first predetermined size suitable for flowing predominantly the liquid phase therethrough; and a plurality of second openings (fi) having a second predetermined size suitable for flowing predominantly the gas phase therethrough; the first openings (Fi) favoring flow therethrough of the liquid phase substantially free of gas bubbles and the second openings (fi) favoring flow therethrough of the gas phase substantially free of the liquid phase, whereby each of the liquid phase and the gas phase are distributed through the reactor (R) in a substantially even, continuous and permanent flow.
The various aspects and advantages of the invention will be made more clear by the description of the embodiment represent in the accompanying drawings in which;
Fig. 1 shows the schematic and partial longitudinal section of a multi¬compartment reactor.
Fig. 2 is an enlarged scale view of the elements forming the plates, comprised in circle A in fig. 1;
Fig 3 is an overhand view of the upper part 2 of an element ELi; Fig. 3 A shows the section along the line A-A of a rectangular ELi element; Fig. 4 is the front view of a plate SPi formed by rectangular element EL" i-EL"n;
Fig. 4A (analogous to fig. 2) is an enlarged view of elements EL" m-1, EL" m, EL"m+1 in fig. 4;
Figs. 5 and 5 A are enlarged views of perforated portions on wall 2 (at right angles to the reactor"s axis) respectively on walls 4, 4" parallel with the axis.

In fig. 1, R shows the central cylindrical shell of the urea reactor and CI, C2, C3 are the three transversal compartments created by the three plates SP1, SP2 and SP3. Atleast one of these plates comprises a plurality of upwardly extending element (ELI-Elm). These upwardly extending elements are
preferably lozenge shaped elements ELI ELn which in fig. 2 are
trapeze-shaped and which in fig. 4 are rectangular by preference.
Fig. 2 shows that every ELi element is shaped like a Greek key, with a wall shaped like an upside down trapeze formed by the side or lesser base 2 at the top, by the greater base at the bottom 3, by the two slanting sides 4 and 4", and by airspace 5. According to the main aspect of the invention, in the embodiment shown in FIG. 2, on the two slanting sides 4 and 4" there are perforations Fi larger than perforations fi on wall 2. Preferably, perforations fi have a diameter which is between 1 and 3.5 mm, most preferably, about 2 to 3 mm, while the large perforations Fi have a diameter which is almost twice that of fi, i.e., 2 to 7 mm, perforations Fi being preferably 3 to 6 mm.
FIG. 3 shows a top view of a wall 2 of a rectangular or trapeze-shaped
element EL"i.
FIG. 4 shows the front view of a flat plate, perforated and formed by
elements from EL"I to EL"n which are rectangular, i.e., with walls 4 and 4"
parallel with the reactor"s axis.
Perforations fi on wall 2 are generally circular as in FIG. 5. On the other
hand, perforations Fi on walls 4 and 4" may be substantially ellipse-shaped
as shown in FIG. 5A as O. They are characterized by a greater axis AM and
by a smaller axis MI.

EXAMPLE
Operations have been carried out by simulation on a reactor whose model has supplied, under nominal design conditions, for a production of about 1800 t/d, a yield of 64% on the total flow (liquid plus gas). If the yield were to be (improperly) estimated on the sole liquid phase, it would be about 65.5%. By increasing production up to about 2300 t/d, a diminution in yield was noticed. This confirms, indirectly, a) that the reactor is far too big, b) that an improvement in transport processes inside the reactor would not only increase the yield, compared to nominal conditions, but would also improve yield which would be maintained throughout notable increases of its potential.
Operations were then continued by simulating with a rigorous mathematical model conditions for a daily production of 23001. in the unmodified reactor. A yield (simulated) was obtained of 61.3%, which, if based (improperly) on the sole liquid phase would yield 63.5%. The absence of a number of data under these conditions does not allow for immediate confirmation, but it would seem that the effective yield predicted by the model under increased production conditions is reasonably close to reality.
Simulation (through the model) of introducing into the reactor new plates in the 16 meters of the lower tangential line of the reactor was then carried out. The model modified in accordance with the invention has shown (for the potential of 2300 t/d already achieved) a yield of 65.8% (+4.5%) absolute) in respect of the total flow (equal to, improperly, 66.7% on the liquid phase, but with a drastic reduction in steam).
It has also been confirmed that such yield can be maintained for further

increases in potential up to 2700 t/d (if that were made possible by the other equipment in the plant). This is a further advantage of the invention.
Consequently, in theory, under the conditions taken into consideration, an increase in yield (simulated) of 4.5% absolute could be obtained and further increases in production would be tolerable.
Some elements resulting from experiments are given below. In the description, which follows, linear dimensions for baffles and for the passage of liquids are indicative. If necessary for construction purposes, they can be varied by about 5|jl0%.
This also applies to the number of perforations per meter both where the liquid phase and the gas phase passes.
On the other hand, the size of the perforations for the gas phase must be considered unchangeable while those for the liquid phase are virtually so.
Finally, it is confirmed that the number of perforations per square for the gas phase and the liquid phase should be read as referred to the areas for the gas phase and the liquid phase and not to the total area (gas plus liquid). Numbering of the plates (suggested, or actually existing, for that part which has not been replaced) begins at the lower tangential line (T.L.) of the reactor (not shown on drawings).
In the same way, when the plates are being installed they should be rotated

alternately (in respect of the dome directrix) by 60°-90° insofar as fastening points allow.
It has been found that, on the whole, the following instructions should be
followed when making the plates:
-the thickness of the metal should not be more than 3.5-4 mm, to permit
punching of the perforations;
-the plates should be oriented alternately, for example, fixing them at right
angles or at 60 °;
-perforations for the installation should be made on that portion of the sheet
metal reserved for the passage of liquid;
-perforations per square meter for the surface intended for the passage of gas
should be understood as referring to the entire surface of the sheet metal,
even that which after being folded becomes lateral (vertical);
-perforations for the gas should be made in equilateral triangular links with a
24 mm pitch;
-after the plate has been shaped it is essential that the plates are closed at the
ends with vertical walls welded to the terminal sections creating a seal to
avoid gas escaping from the sides;
-to make up for the thinness suitable supports or stiffeners can be applied to
the sheet metal after perforating and shaping;
-the gas should be introduced into the lower part through a horizontal tube
with multiple perforations set at right angles to the lowest plate: if this were
not possible, it would become necessary to arrange two plates, close to one
another (300-500 mm) which would obtain the same result (since the lower
plate would act as a distributor for the upper plate).

The plates should be at a distance of about 2.4 m.
Perforations for the gas could, in principle, be varied from one plate to the other, with a perforated area decreasing from bottom towards the top; however, with the plates arranged according to the invention, it is possible to maintain even perforations equal to the maximum perforations required for the lower plate. This simplifies construction and installation procedures. In the upper plates, the vapors (gas) are gradually decreasing, resulting in an increase of the level of the liquids inside the domes and a decrease of the head of gas (part of the perforations for the passage of gas will therefore be used by the liquid).
In a preferred embodiment:
-perforations for the gas (in the present case) were 2000 holes/(square meter
of relative area) with a diameter 0=3 mm; arranged as an equilateral triangle
(preferred arrangement), this means a distance between perforations, for
example, of 24 mm (and a fraction of perforated area, on the area intended
for gas, of 1.4%) (FIG. 5);
perforations for the liquid (in the present case), 600 holes/(square meter of
relative area) with diameter 08 mm, arranged as an equilateral triangle with
a distance of 43 mm. Where oval perforations are used (FIG. 5A), their axes
are 4 mm-6 mm, interspersed in the same way (with a fraction of perforated
area of about 3% of the area for the liquid).
Obviously, the metallic strips bearing the perforations, after being folded and installed, should be bolted one to another, leaving an edge for the alternating overlap from one dome to the next.

For the sake of clarity and illustrative simplicity, the invention has been described with reference to the embodiments shown in the drawings. These however are subject to all those variations, substitutions, and modifications, etc. which being available to the average technician in this field can be considered as falling naturally within the wider scope and spirit of the invention.
The Indian Patent 183121 (24/MAS/92) relates to reactor and a method for producing urea by reacting a liquid phase including ammonia and a gas phase including carbon dioxide separating the liquid phase for the gas phase by means of a plurality of plates.

WE CLAIM:
1. A device for producing urea, comprising a plurality of plates (SP1 -SP3) insertable within the internal space of a reactor (R) for producing urea, wherein at least one of said plates (SP1 -SP3) comprises: a plurality of first openings (Fi) having a first predetermined size suitable for flowing predominantly the liquid phase therethrough; and a plurality of second openings (fi) having a second predetermined size suitable for flowing predominantly the gas phase therethrough; the first openings (Fi) favoring flow therethrough of the liquid phase substantially free of gas bubbles and the second openings (fi) favoring flow therethrough of the gas phase substantially free of the liquid phase, whereby each of the liquid phase and the gas phase are distributed through the reactor (R) in a substantially even, continuous and permanent flow.
2. The device according to claim 1, wherein at least one of said plates (SP1 -SP3) comprises a plurality of upwardly extending elements (ELI -ELn), said at least one plates (SP1 -SP3) being open at the bottom, and each said element (ELI - ELn) comprises: two perforated side walls (4, 4") defining a first area containing said first openings (Fi) of predetermined size for flow of the liquid phase substantially free of gas bubbles, and a perforated top wall (2) defining a second area containing said second openings (fi) having a second predetermined size for flow of the gas phase substantially free of the liquid phase.

3. The device according to claim 2, wherein said second openings (fi) in the top wall (2) are smaller in size than the first openings (Fi) in the side walls (4, 4").
4. The device according to claim 2, wherein at least one of said plates (SP1 -SP3) comprises a plurality of elements (Ell -ELn) having rectangular cross-sections.
5. The device according to claim 2, wherein at least one of said plates (SP1 -SP3) comprises a plurality of elements (ELI -ELn) having trapezoidal cross-sections.
6. The device according to claim 2, wherein the first openings (Fi) in the side walls (4, 4") have a diameter of 2 to 7 mm and the second openings (fi) in the top wall (2) have a diameter of 1 to 3.5 mm.
7. The device according to claim 6, wherein the first openings (Fi) in the side walls (4, 4") have a diameter of from 3 to 6 mm and the second openings (fi) in the top wall (2) have a diameter of from 2 to 3 mm.
8. The device according to claim 2, wherein the first openings (Fi) in the side walls (4, 4") are elliptical.

9. The device according to claim 2, wherein the second openings (fi) in the
top wall (2) are round.
10. A device for producing urea, substantially as hereinabove described and
illustrated with reference to the accompanying drawings.

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Patent Number

198081

Indian Patent Application Number

1389/MAS/1996

PG Journal Number

20/2006

Publication Date

19-May-2006

Grant Date

03-Feb-2006

Date of Filing

06-Aug-1996

Name of Patentee

M/S. UREA CASALE S. A.

Applicant Address

VIA DELLA POSTA 4, CH-6900 LUGANO.

Inventors:

#	Inventor's Name	Inventor's Address
1	MARIO DENTE	CORSO SEMPIONE 38, I-20154 MILANO.
2	SERGIO BOZZANO	VIA DE GASPERI 13, I-20057 MILANO.

PCT International Classification Number

N/A

PCT International Application Number

N/A

PCT International Filing date

PCT Conventions:

#	PCT Application Number	Date of Convention	Priority Country
1			NA