Title of Invention

A PROCESS OF GASEOUS ACID CATALYSIS

Abstract

A process of gaseous acid catalysis characterised in that it includes the steps of introducing a reactant in solid form into a reactor, the reactant including one or more hydroxyl groups, introducing superheated steam into the reactor until the reactant is dry and the temperature within the reactor is above that of the dewpoints of both water and the catalyst to be used; introducing the acid together with the superheated steam into the reactor by means of a vaporiser; and condensing the gas formed.

Full Text

FORM-2 THE PATENTS ACT, 1970 (39 of 1970) COMPLETE Specification (Section 10; rule 13) A PROCESS OF GASEOUS ACID CATALYSIS INTERNATIONAL FURAN TECHNOLOGY (PTY) LTD. of Suite 8, 15 The Boulevard, Westway Office Park, 3630, Kwa Zulu Natal, Republic of South Africa, a South African Company GRANTED 6-12-2004 THE FOLLOWING SPECIFICATION PARTICULARLY DESCRIBES THE NATURE OF THIS INVENTION AND THE MANNER IN WHICH IT IS TO BE PERFORMED:- 6 DEC 2004 TECHNICAL FIELD OF THE INVENTION This invention relates to a process of gaseous acid catalysis and in particular a process of gaseous acid catalysis for the conversion of pentose or pentosan to furfural. BACKGROUND ART Acid catalysis, a common reaction mechanism in organic chemistry, implies the involvement of oxonium, or hydronium, ions, H30+. "Acid catalysis" is inherently understood to be a process that occurs in aqueous solution. As far as the applicant is aware nobody seems to have used a gas as an acid catalyst, and with good reason. As shown in Figure 1, gases are not ionized until very high temperatures are reached. As can be seen, there is no significant thermal ionization below 2500°C for water and below 5000°C for HC1. Ionization by cosmic rays and ambient radioactivity has also been shown to be negligible, together amounting to no more than 10 ion pairs/(s cm3) with a life span of 70 s. Thus, gases at all but extremely high temperatures may be considered completely nonionized, as demonstrated by their being perfect electrical insulators. Obviously, a nonionized gas cannot be an "acid catalyst", therefore, it has been the universal belief that acid-catalyzed processes must be carried out in the liquid phase. However, recent studies of stratospheric chemistry and the depletion of the ozone layer have shown that HC1 vapour, usually stable, becomes ionized in the presence of ice crystals that are abundant in the stratosphere. HC1 and water vapour molecules are strongly adsorbed on the surface of the ice crystals. In the state of adsorption, each HC1 molecules reacts preferentially with four water molecules to form an ionized cluster, H30+(H20)3Cr, in which the three water molecules form the equatorial plane of a trigonal bipyramid, with CI" and H30+ ions at the apexes. The chlorine atom carries a charge of-0.80 e and the oxonium ion a charge of+0.85 e, so that the electrical activity of the cluster is almost equal to that of free Cr and H30+ ions. The role of the solid surface is to permit HC1 molecules to come into contact with four water molecules, which is not possible via collisions in a gas phase devoid of adsorbing surfaces. It is therefore one object of this invention to provide a process for gaseous acid catalysis. The applicant has further noted the similarity between ice crystals and other solids having multiple polar hydroxyl groups, for example sugars, and in particular pentose or pentosan. It is therefore a further object of this invention to provide a process for gaseous acid catalysis catalyzed hydrolysis of sugars to form aldehydes and in particular, conversion of pentosan and pentose to furfural. USA-4001283 discloses the preparation of furfural from pentosan -containing materials using steam and a volatile acid catalyst (hydrogen chloride). However under these conditions, (steam as opposed to the use of super-heated steam) HC1 is in solution and accordingly does not behave as a gaseous catalyst as described in this invention. DISCLOSURE OF THE INVENTION According to the invention, a process of gaseous acid catalysis includes the steps of introducing a reactant in solid form into a reactor, the reactant including one or more hydroxyl groups; introducing superheated steam into the reactor until the reactant is dry and the temperature within the reactor is above that of the dewpoints of both water and the catalyst to be used; introducing the acid into the reactor together with the superheated steam by means of a vaporiser; and condensing the gas formed. In the preferred form of the invention, the reactant is capable of forming an ionised cluster complex with water and at least a portion of the acid. Also in the preferred form, the reaction is carried out at atmospheric pressure. The reactant should be completely dry. In the preferred form, the acid is hydrochloric acid. In this form of the invention, the reaction must be carried out at a temperature above the boiling point of the maximum HCl - H20 azeotrope. This typically occurs at 20.2 wt% of HCl with a boiling point of 108,6°C and accordingly the reaction should be carried out above this temperature. In one form of the invention, the reactant is sugar. In one form of the invention, the reactant is pentosan and/or pentose and the solid substance is a comminuted raw material high in pentosan content, for example sunflower stems, corn cobs or bagasse. DESCRIPTION OF AN EXAMPLE OF THE INVENTION A typical gaseous acid catalysis process using hydrochloric acid is illustrated in Figure 2. Reactor 1 is charged with comminuted raw material of high pentosan content, such as sunflower stems, corn cobs, or bagasse. Steam at atmospheric pressure is passed through a superheater 2 typically fuelled by combustion gas, and this steam is then passed through the charge to first completely dry the charge and then heat it to a temperature far above the maximum atmospheric dew point of hydrochloric acid. The charge will heat rapidly once the moisture has been stripped from it. When the desired temperature is reached, a small quantity of hydrochloric acid is continuously dispersed into the superheated steam by means of a vaporizer 3 to give the gas stream an HC1 content of approximately 1.5 wt%. The gas stream leaving the reactor is liquefied in a condenser 4, and the condensate is collected in a buffer tank 5 before it enters a separation plant 6 that isolates furfural, low boiling compounds, and carboxylic acids and recovers HC1 as its azerotrope with water. This hydrochloric acid is used to feed the vaporiser 3, so that the catalyst is contained in a closed circuit. The "pervaporisation" of the charge is continued until nomore furfural is produced. Then, the residue is discharged under nitrogen, to prevent self-ignition, and a new batch is started. When this reaction is carried out at 155°C, the applicant found that the existing gas stream was heavily loaded with furfural, low boiling compounds and carboxylic acids. What is most surprising about this result is the presence of the furfural as a gas even though the process is carried out at a temperature below its boiling point (161.7°C). An important advantage of this new process is that the absence of a liquid phase greatly increases the furfural yield. In convention furfural process, the furfural generated dissolves in the liquid phase, where, under the catalyzing influence of oxonium ions, it undergoes loss reactions with itself and with intermediates of the pentose-to-furfural conversion. In addition, with sulphuric acid as the customary catalyst, there are losses by sulfontation. Consequently, the yield in conventional furfural plants is only on the order of 50%. By contrast, in gaseous acid catalysis, with no liquid phase in which to dissolve, the generated furfural is instantly vaporised and loss reactions are avoided. In a laboratory test, yields of the order of 95% have been achieved. In conventional furfural processing, high pressures are needed to keep the aqueous catalyst in the liquid state, and the customary catalyst, sulphuric acid,is nonvolatile, so that it is lost in the residue where it presents a disposal problem. As compared to this conventional processing, the new gaseous catalysis process has the following advantages: 1. At any chosen temperature, the process can be carried out at atmospheric pressure. 2. As the H20/HC1 catalyst is used far above its dew point, there is no corrosion, so that the reactor can be made of mild steel. 3. The acid portion of the catalyst can be completely recovered, to be run in a closed circuit, so that there is no acid consumption and no acid disposal problem. Known technology is available for the acid recovery. 4. The residue is dry and free of acid, thus being eminently suited for a simple combustion without any problems. By partial combustion in air, it is also possible to use the residue for the manufacture of "producer gas" consisting mostly of carbon monoxide, hydrogen and nitrogen. 5. The yield is close to 100 percent as there is no liquid phase where loss reactions could take place, Yields of up to 95.8 percent have been measured. It should be noted that although an example of a batch process is described hereinabove, the applicant submits that a continuous process may be used. , We Claim: 1. A process of gaseous acid catalysis characterised in that it includes the steps of introducing a reactant in solid form into a reactor, the reactant including one or more hydroxyl groups, introducing superheated steam into the reactor until the reactant is dry and the temperature within the reactor is above that of the dewpoints of both water and the catalyst to be used; introducing the acid together with the superheated steam into the reactor by means of a vaporiser; and condensing the gas formed. 2. A process according to claim 1 characterised in that the reactant is capable of forming an ionised cluster complete with water and at least a portion of the acid. 3. A process according to claim 1 or claim 2 characterised in that the reaction is carried out at atmospheric pressure. 4. A process according to any of the above claims characterised in the acid is hydrochloric acid. 5. A process according to claim 4 characterised in that the reaction is carried out at a temperature above the boiling point of the maximum HC1- H20 azeotrope. 6. A process according to claim 1 characterised in that the reactant is a sugar. 7. A process for the manufacture of aldehydes from sugars characterised in that the hydrolysis of the sugar is catalysed by a method of gaseous acid catalysis according to claim 1. 8. A process for the manufacture of furfural from pentosan according to claim 6 characterised in that the hydrolysis of pentosan and/or pentose and subsequent dehydration to furfural is catalysed by gaseous hydrochloric acid according to the method of catalysis of claim 1. 9. A process for the manufacture of furfural according to claim 6 characterised in that the hydrochloric acid is recycled as its azeotrope with water. 10.A process for the manufacture of furfural according to claim 6 characterised in that the reaction is carried out at 155°C. 11.A process for the manufacture of furfural according to claim 6 characterised in that the yield of furfural is greater than 90%. 12.A process according to claim 6 characterised in that it is a continuous. Dated 21st day of March 2003. OF R.K.DEWAN & COMPANY APPLICANTS' PATENT ATTORNEY

Documents:

320-MUMNP-2003-ABSTRACT(21-3-2003).pdf

320-MUMNP-2003-ABSTRACT(GRANTED)-(29-3-2007).pdf

320-MUMNP-2003-ASSIGNMENT(7-7-2004).pdf

320-mumnp-2003-cancelled pages(21-3-2003).pdf

320-MUMNP-2003-CLAIMS(21-3-2003).pdf

320-MUMNP-2003-CLAIMS(GRANTED)-(29-3-2007).pdf

320-mumnp-2003-claims(granted)-(6-12-2004).doc

320-mumnp-2003-claims(granted)-(6-12-2004).pdf

320-mumnp-2003-correspondence(6-12-2004).pdf

320-MUMNP-2003-CORRESPONDENCE(IPO)-(17-5-2007).pdf

320-mumnp-2003-correspondence(ipo)-(30-9-2004).pdf

320-MUMNP-2003-DESCRIPTION(COMPLETE)-(21-3-2003).pdf

320-MUMNP-2003-DESCRIPTION(GRANTED)-(29-3-2007).pdf

320-mumnp-2003-drawing(21-3-2003).pdf

320-MUMNP-2003-DRAWING(GRANTED)-(29-3-2007).pdf

320-MUMNP-2003-FORM 1(21-3-2003).pdf

320-mumnp-2003-form 13(2-11-2004).pdf

320-mumnp-2003-form 19(28-5-2003).pdf

320-mumnp-2003-form 1a(30-6-2004).pdf

320-mumnp-2003-form 1a(6-12-2004).pdf

320-MUMNP-2003-FORM 2(COMPLETE)-(21-3-2003).pdf

320-MUMNP-2003-FORM 2(GRANTED)-(29-3-2007).pdf

320-mumnp-2003-form 2(granted)-(6-12-2004).doc

320-mumnp-2003-form 2(granted)-(6-12-2004).pdf

320-MUMNP-2003-FORM 2(TITLE PAGE)-(21-3-2003).pdf

320-MUMNP-2003-FORM 2(TITLE PAGE)-(GRANTED)-(29-3-2007).pdf

320-MUMNP-2003-FORM 3(21-3-2003).pdf

320-mumnp-2003-form 3(30-6-2004).pdf

320-mumnp-2003-form 5(30-6-2004).pdf

320-mumnp-2003-form 6(29-03-2007).pdf

320-mumnp-2003-form 6(30-6-2004).pdf

320-mumnp-2003-pct-ipea-409(21-3-2003).pdf

320-mumnp-2003-pct-isa-210(21-3-2003).pdf

320-mumnp-2003-petition under rule 137(30-6-2004).pdf

320-mumnp-2003-petition under rule 138(30-6-2004).pdf

320-mumnp-2003-power of attorney(28-5-2003).pdf

320-MUMNP-2003-SPECIFICATION(AMENDED)-(6-12-2004).pdf

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