PROCESS FOR OBTAINING A FORMATE FROM A REACTION MIXTURE

Abstract

The invention relates to a process for obtaining a formate from a reaction mixture (10) in which a polyoxometallate ion, which acts as a catalyst, is in contact with an organic material at a temperature below 120° C. to produce formic acid in an aqueous solution, with the following steps. a) separating a mixture of formic acid and water from the reaction mixture by reverse osmosis and/or as vapor (18), the vapor (18) subsequently being condensed, and b) reacting the formic acid with a hydroxide (24) in aqueous solution to produce a solution of a formate.

Claims

1-11. (canceled)

12. A method for obtaining a formate from a reaction mixture (10), in which a polyoxometallate ion, which acts as a catalyst, of the general formula [PMo.sub.xV.sub.yO.sub.40].sup.n− is in contact with an organic material at a temperature below 120° C. to produce formic acid in an aqueous solution, wherein 6≦x≦11, 1≦y≦6, x+y=12 and 3<n<10, wherein n, x and y are each a whole number, which method comprises the following steps: a) separating a mixture of formic acid and water from the reaction mixture by reverse osmosis and/or as vapor (18), the vapor 18 subsequently being condensed and b) reacting the formic acid not separated from the water with a hydroxide (24) in aqueous solution to produce a solution of a formate, wherein the organic material is an alpha-hydroxyaldehyde, an alpha-hydroxycarboxylic acid, a carbohydrate, or a glycoside.

13. The method according to claim 12, wherein the solution produced in step b) is concentrated in a step c) by separation of water (14) by reverse osmosis and/or partial or complete evaporation of the water (14).

14. The method according to claim 12, wherein further water and/or the water (14) separated in step c) is added to the reaction mixture (10) to compensate for the water separated in step a).

15. The method according to claim 12, wherein further organic material (12) is added to the reaction mixture (10) to compensate for the reacted organic material.

16. The method according to claim 12, wherein the maintenance of contact and/or separation as vapor (18) according to step a) occurs at a temperature of 15 to 119.5° C., in particular 40 to 95° C., in particular 50 to 85° C., in particular 55 to 85° C., in particular 60 to 83° C.

17. The method according to claim 12, wherein the separation as vapor (18) according to step a) takes place at a pressure that is reduced with respect to atmospheric pressure.

18. The method according to claim 12, wherein the condensation of the vapor (18) according to step a) occurs by introducing the vapor (18) into the water, an aqueous solution, or the aqueous solution according to step b).

19. The method according to claim 12, wherein the hydroxide (24) is ammonium hydroxide, aluminum hydroxide, copper hydroxide, nickel hydroxide, an alkaline earth metal hydroxide, an alkali metal hydroxide, calcium hydroxide, magnesium hydroxide, sodium hydroxide, potassium hydroxide, or cesium hydroxide.

20. The method according to claim 12, wherein the hydroxide (24) in step b) is used in such a stoichiometric ratio to the formic acid that it is reacted completely or almost completely.

21. The method according to claim 12, wherein n=3+y.

Description

[0020] The invention is explained more closely below with reference to a drawing and an exemplary embodiment:

[0021] Wherein:

[0022] FIG. 1 is a schematic representation of a simply designed process according to the invention and

[0023] FIG. 2 is a schematic representation of a further embodiment of the process according to the invention.

[0024] The schematic representation according to FIG. 1 shows a first vessel 8 containing a reaction mixture 10. The reaction mixture 10 comprises water, polyoxometallate ions as catalyst, an organic material, and formic acid produced from the organic material by means of the catalyst. The reaction mixture is maintained at a temperature range between 78° C. and 82° C. by means of a heat exchanger 16. Depending on the substrate, the catalyst used, amount of catalyst used, and degree of oxidation of the catalyst used it may be necessary to increase or decrease the heat supply to the reaction mixture. The pressure in the reaction mixture is reduced far enough below atmospheric pressure that a formic acid vapor-water vapor mixture 18 evaporates effectively in this temperature range. The formic acid vapor-water vapor mixture 18 is condensed by means of the cooler 20 to the formic acid-water mixture 22, which is stored in a second vessel 23. Further organic material 12 is added to compensate for the organic material reacted in producing the formic acid.

[0025] Hydroxide 24, for example in the form of a potassium hydroxide solution or a solid potassium hydroxide, is added to the formic acid-water mixture 22 in the second vessel. In the second vessel 23 this effects an exothermic neutralization of the formic acid, producing a formate. If and to the extent that it is still necessary because of the exothermic reaction, the resulting formate-water mixture 26 is heated by means of the heat exchanger 16, so that water vapor 14 is produced and after condensation in a cooler, not shown here, can be returned to the reaction mixture 10. Formate or a concentrated formate solution 28 remains in the second vessel and can be transferred to a transport trolley or tank truck 30 for removal.

[0026] In the further embodiment of the process according to the invention according to FIG. 2, a portion of the reaction mixture 10 is removed from the vessel 8, which contains the reaction mixture 10, maintained in a temperature range of around 92° C. to 97° C. by means of a heat exchanger, not shown, and is transferred to a first distillation vessel 13. There the reaction mixture 10 is maintained at lower than atmospheric pressure in a temperature range of around 78° C. to 82° C. by means of a heat exchanger, likewise not shown here, so that a formic acid vapor-water vapor mixture 18 is produced. The formic acid vapor-water vapor mixture 18 escapes the first distillation vessel 13 via a pipe and is condensed to a formic acid-water mixture 22 in a cooler, not shown here, and delivered to the second vessel 23. The remaining water, polyoxometallate ions, and organic material as well as a residue 19 containing a remnant of formic acid is returned to the reaction mixture 10 in the first vessel. Further organic material 12 is supplied to the reaction mixture 10 to compensate for the organic material reacted in the reaction.

[0027] A hydroxide 24 is added to the formic acid-water mixture 22 in the second vessel 23, so that a formate is produced during the resultant neutralization. Since this neutralization is exothermic, the formate-water mixture is heated in the process. The resulting water vapor 14 can be returned to the reaction mixture 10 after condensation by means of the cooler, not shown here. The formate-water mixture from the second vessel 10 is supplied to a second distillation vessel 27. If and to the extent that it is necessary, the formate-water mixture 26 is heated by means of a heater, not shown here, so that the water 14 contained in the formate-water mixture 26, possibly under reduced pressure, escapes as water vapor. After condensation in a cooler, not shown here, the water 14 is supplied to the reaction mixture 10. The formate-water mixture 26 can be vaporized in the second distillation vessel 27 until the formate is present in crystalline form. The remaining formate or concentrated formate solution 28 is transferred from the second distillation vessel 27 to a transport trolley or tank truck 30 for removal.

[0028] The process according to FIG. 2 is higher in equipment expense than the process according to FIG. 1, but has the advantage that the temperature for evaporation of the formic acid vapor-water vapor mixture 18 can be chosen independently of the reaction temperature in the first vessel 8. Thus a higher temperature and therefore higher reaction speed in the first vessel 8 can be selected than is favorable for evaporation of a formic acid vapor-water vapor mixture 18 with the largest possible proportion of formic acid.

REFERENCE SIGNS

[0029] 8 first vessel [0030] 10 reaction mixture [0031] 12 further organic material [0032] 13 first distillation vessel [0033] 14 water/water vapor [0034] 16 heat exchanger [0035] 18 formic acid vapor-water vapor mixture [0036] 19 residue [0037] 20 cooler [0038] 22 formic acid-water mixture [0039] 23 second vessel [0040] 24 hydroxide [0041] 26 formate-water mixture [0042] 27 second distillation vessel [0043] 28 concentrated formate solution [0044] 30 tank truck