GB2201413A - Recovery of volatile organic compounds from a biomass - Google Patents
Recovery of volatile organic compounds from a biomass Download PDFInfo
- Publication number
- GB2201413A GB2201413A GB8703984A GB8703984A GB2201413A GB 2201413 A GB2201413 A GB 2201413A GB 8703984 A GB8703984 A GB 8703984A GB 8703984 A GB8703984 A GB 8703984A GB 2201413 A GB2201413 A GB 2201413A
- Authority
- GB
- United Kingdom
- Prior art keywords
- volatile organic
- organic compound
- membrane
- biomass
- water
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn
Links
- 239000012855 volatile organic compound Substances 0.000 title claims abstract description 42
- 239000002028 Biomass Substances 0.000 title claims abstract description 26
- 238000011084 recovery Methods 0.000 title claims abstract description 9
- 239000012528 membrane Substances 0.000 claims abstract description 55
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 29
- 238000000034 method Methods 0.000 claims abstract description 27
- 230000008569 process Effects 0.000 claims abstract description 24
- 238000000855 fermentation Methods 0.000 claims abstract description 20
- 230000004151 fermentation Effects 0.000 claims abstract description 20
- 239000012466 permeate Substances 0.000 claims abstract description 15
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 24
- 239000007789 gas Substances 0.000 claims description 24
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 12
- 239000001569 carbon dioxide Substances 0.000 claims description 12
- 238000011144 upstream manufacturing Methods 0.000 claims description 10
- 239000008246 gaseous mixture Substances 0.000 claims description 9
- 239000002250 absorbent Substances 0.000 claims description 8
- 230000002745 absorbent Effects 0.000 claims description 8
- 239000011159 matrix material Substances 0.000 claims description 8
- 238000005373 pervaporation Methods 0.000 claims description 8
- 239000012465 retentate Substances 0.000 claims description 8
- 239000007788 liquid Substances 0.000 claims description 6
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 150000002894 organic compounds Chemical class 0.000 claims description 4
- 229920000435 poly(dimethylsiloxane) Polymers 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims 1
- 230000005494 condensation Effects 0.000 claims 1
- 238000002474 experimental method Methods 0.000 description 10
- 230000000052 comparative effect Effects 0.000 description 7
- 238000010438 heat treatment Methods 0.000 description 5
- IDGUHHHQCWSQLU-UHFFFAOYSA-N ethanol;hydrate Chemical group O.CCO IDGUHHHQCWSQLU-UHFFFAOYSA-N 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 229920000642 polymer Polymers 0.000 description 4
- -1 rubbers or resins Chemical class 0.000 description 4
- 239000004205 dimethyl polysiloxane Substances 0.000 description 3
- 238000004821 distillation Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 230000004888 barrier function Effects 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 238000009792 diffusion process Methods 0.000 description 2
- 229920001971 elastomer Polymers 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000007710 freezing Methods 0.000 description 2
- 230000008014 freezing Effects 0.000 description 2
- 239000000659 freezing mixture Substances 0.000 description 2
- 230000035699 permeability Effects 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000005060 rubber Substances 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229920002261 Corn starch Polymers 0.000 description 1
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 1
- 240000004808 Saccharomyces cerevisiae Species 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 235000013405 beer Nutrition 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- FACXGONDLDSNOE-UHFFFAOYSA-N buta-1,3-diene;styrene Chemical compound C=CC=C.C=CC1=CC=CC=C1.C=CC1=CC=CC=C1 FACXGONDLDSNOE-UHFFFAOYSA-N 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- VTVVPPOHYJJIJR-UHFFFAOYSA-N carbon dioxide;hydrate Chemical compound O.O=C=O VTVVPPOHYJJIJR-UHFFFAOYSA-N 0.000 description 1
- 238000005266 casting Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000008120 corn starch Substances 0.000 description 1
- 229940099112 cornstarch Drugs 0.000 description 1
- 229910002026 crystalline silica Inorganic materials 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 229920001973 fluoroelastomer Polymers 0.000 description 1
- 229920005560 fluorosilicone rubber Polymers 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229920000098 polyolefin Polymers 0.000 description 1
- 229920002635 polyurethane Polymers 0.000 description 1
- 239000004814 polyurethane Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 229920002379 silicone rubber Polymers 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 238000000807 solvent casting Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 229920000468 styrene butadiene styrene block copolymer Polymers 0.000 description 1
- 235000000346 sugar Nutrition 0.000 description 1
- 150000008163 sugars Chemical class 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
- 229920001169 thermoplastic Polymers 0.000 description 1
- 239000004416 thermosoftening plastic Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Process for the recovery of a volatile organic compound prepared by a fermentation process, e.g. ethanol, from a biomass also containing water by taking up volatile organic compound and water from the biomass into a stripping gas, contacting the stripping gas with a membrane which is selectively permeable to the volatile organic compound and recovering a permeate comprising the volatile organic compound from the other side of the membrane.
Description
PROCESS FOR THE RECOVERY OF VOLATILE ORGANIC
COMPOUNDS FROM A BIOMASS
The invention relates to a process for the recovery of a volatile organic compound from a biomass containing said volatile organic compound and water and in which biomass said volatile organic compound has been produced by fermentation of fermentable organic compounds by a fermenting agent.
It has been known for many years to carry out such processes by means of distillation, usually after removal of solid substances from the biomass. For example, a biomass containing ethanol gives after removal of solid substances a so-called "dilute beer", which can be separated by distillation into an overhead fraction having the composition of the ethanol-water azeotrope, and an aqueous bottom fraction.
A disadvantage of this known recovery process is that distilling all of the liquid present -in the mass consumes much energy.
It is. an object of the present invention to reduce the energy consumption required for the recovery of said volatile organic compounds.
Accordingly, the invention provides a process for the recovery of a volatile organic compound from a biomass containing said volatile organic compound and water and in which biomass said volatile organic compound has been produced by fermentation of fermentable organic compounds by a fermenting agent, which process comprises stripping said biomass with a stripping gas, withdrawing a gaseous mixture comprising stripping gas, volatile organic compound and water from the biomass, contacting said withdrawn gaseous mixture with the upstream side of a membrane which is selectively permeable to said volatile organic compound and recovering a permeate comprising said volatile organic compound from the downstream side of the membrane.
A membrane can be defined herein as a barrier separating two gases or vapours, which barrier prevents hydrodynamic flow therethrough, so that transport between the gases or vapours is effected by sorption and diffusion. The driving force for transport through the membrane is vapour pressure, concentration or a combination of both. During operation permeate molecules, i.e. said volatile organic compound, dissolve into such a membrane at its upstream surface followed by molecular diffusion down its concentration gradient to the downstream surface of the membrane. At the downstream surface of the membrane the permeate becomes available in the vapour state and is condensed. The property of the membrane describing the rate of transport is called its permeability.
Membranes can be distinguished as to their microstructural forms in porous ones and non-porous or dense ones. The membranes used in the process according to the present invention are generally dense membranes. Dense membranes have the ability to transport small molecules selectively; even molecules of the same size can be separated when their solubilities and/or diffusivities in the membrane differ significantly. To attain acceptable transport rates, required for commercial application in separation processes where productivity is of paramount concern, it is necessary to make such membranes ultrathin.This can be construed from the following equation applicable for gas separation
L wherein N is the permeation rate, P is the permeability, i.e. the product of solubility and
diffusivity,
(P1-P2) is the vapour pressure difference over the membrane, ana
L is the membrane thickness.
From the above it will be clear that the rate of permeation per unit surface for a given material of the membrane and a given permeate depends (apart from the pressure and/or concentration difference) upon the thickness of the membrane
The membranes which are used in the process according to the present invention are selectively permeable to said volatile organic compound.The selectivity (α) of the membrane is defined herein as the product of Y/X and X/Y wherein X is the concentration of the volatile organic compound in the gaseous mixture withdrawn from the biomass, X2 is the concentration of the water in the gaseous mixture withdrawn from the biomass, Y is the concentration of the volatile organic compound in the permeate recovered at the other side of the membrane and Y2 is the concentration of the water in the permeate recovered at the other side of the membrane.
A main advantage of the process according to the invention is that separating volatile organic compound from the permeate requires less energy than from the gaseous mixture withdrawn from the biomass or from the biomass itself, the former gaseous mixture having a higher content of volatile organic compound than the latter.
According to a preferred embodiment of the present invention the membrane comprises a matrix in which an absorbent is present that selectively absorbs said volatile organic compound. As matrix a wide variety of polymers can be applied. These polymers may either comprise thermoplastics, such as polyalkenes or thermohardening compounds such as rubbers or resins, for example silicone rubbers (for example polydimethylsiloxane), fluoro-elastomers (for example fluorosilicone elastomers), polyurethanes and styrenebutadiene-styrene rubbers. Polydimethylsiloxane is preferred as a matrix. The absorbent which is present in the matrix is preferably a silicalite.A "silicalite" is defined herein as a crystalline silica polymorph having in the as-synthesized form a specific gravity at 25 OC of 1.99r0.05 -g/cm9 as measured by water displacement, and a mean refractive index of 1.48+0.01. In the form obtained after calcination for one hour in air at 600 OC these values are 1.70+0-.05 g/cm3 and 1.39i0.01, respectively. A process for the preparation of silicate is described in US patent specification
No. 4,061,724. The absorbent is suitably present in the membrane in a content in the range of from 20 to 80% by weight, calculated on the total of absorbent and matrix, a higher absorber content allowing a higher permeation rate. However, contents outside this range are not excluded.The absorbent suitably has a particle size below 10 m and preferably below 2 um.
Preferably, the membrane has a thickness in the range of from 0.1 to 200 m and, more preferably, from 0.5 to 50 m in order to attain a relatively high permeation rate.
The membranes being used according to the invention can have many configurations, for example it may have the form of substantially flat sheets or hollow fibres or it may be spirally wound or tubular.
Between both sides of the membrane a pressure differential is suitably maintained. The gaseous mixture being contacted with the upstream side of the membrane is preferably saturated or almost saturated with volatile organic compound and the pressure being maintained at the downstream side of the membrane is suitably as low as possible and will usually be sub-atmospheric.
The temperature at which the membrane is applied may vary within a wide range, provided that the membrane can withstand the operating conditions. A temperature in the range of from 0 C to 200 C is suitable in most cases whereas a temperature from 20 0C to 100 C is preferred.
A retentate is recovered from the upstream side of the membrane and substantially consists of stripping gas and water vapour; a small amount of volatile organic compound may be present. This retentate may be given any desired destination, but preferably a portion thereof and, more preferably, all of it, is used for stripping said biomass. The water vapour originating from the retentate and present in the stripping gas reduces the amount of water that evaporates from the biomass and, hence, reduces energy consumption. If desired, a make-up stream of stripping gas may be supplied to the retentate.
The process according td the 'present: inventibn is applicable to the recovery of any volatile og-.'niQ' compound prc":iuc'ec b; fermentation. According to a preferred embodiment ethanol is recovered. Examples of fermentable organic compounds are cornstarch and sugars, fermentation thereof involving production of ethanol and carbon dioxide. Yeast is an example of a fermenting agent. Any stripping gas that the biomass can withstand may be used; it is an attractive feature of the invention that carbon dioxide can be used, a gas which usually becomes available during fermentation.
Fermentation is usually carried out at a temperature in the range of from 30 CC to 100 C.
The membranes which are used in the process according to the present invention may be prepared by any method known in the art. A suitable method is solvent casting which involves forming a solution of a polymer or a prepolymer of the desired membrane matrix in a solvent in which particles of the desired absorbent have been dispersed, a surface active agent usually being present, and casting the solution onto a porous support to produce a thin layer which is subsequently dried by evaporation of the solvent present in the solution of the polymer or prepolymer.
The permeate recovered from the downstream side of the membrane has an enhanced content of volatile organic compound and also contains water. The volatile organic compound may be isolated from the permeate in any desired manner. According to a preferred embodiment of the invention the volatile organic compound is recovered from the permeate by cooling to separate the permeate into a condensate containing volatile organic compound and water.
This condensate may be separated into volatile organic compound and water in any desired manner, for example by means of distillation.
Suitably, the condensate is separated by contacting with the upstream side of a pervaporation membrane which is selectively permeable to water vapour, recovering liquid volatile organic compound from the upstream side of the pervaporation membrane and withdrawing water vapour from the downstream side of the pervaporation membrane. An example of a pervaporation membrane is given in the article "Pervaporation Membranes. An economical method to replace conventional dehydration and rectification columns in ethanol distilleries," by A.H. Ballweg c.s., presented at the fifth international symposium on alcohol fuel technology, 13-18-May, 1982, Auckland, New Zealand.
The following Examples further illustrate the invention. The experiments are carried out in an experimental set-up as shown in the accompanying drawing.
Comparative Experiments A and B
A fermentation tower 1 (see the drawing) having a length of 100 cm and a width of 1 cm is fed with a fermentation reaction mixture. The liquid in the fermentation tower 1 contains 95% by weight of water and 5% by weight of ethanol in Comparative Experiment
A and 90% water and 10% ethanol in Comparative Experiment B. The tower l is surrounded by a heating jacket 2 into which a heating medium is supplied through a line 3. Used heating medium is discharged from the heating jacket 2 via a line 4. The heating medium keeps the tower at a temperature of 60 OC.
Carbon dioxide (13 Nl/h) is introduced into the bottom of the fermentation tower 1 via a line 5 and a glass filter 6, which evenly distributes the carbon dioxide through the biomass present in the fermentation tower 1. The carbon dioxide bubbles through the biomass present in the tower 1 and a gas containing carbon dioxide, water and ethanol is withdrawn from the fermentation tower 1 via a line 7 and a line 8. The gas is then passed through a valve 9 which, in this experiment, is open and through a line 10 into a cylindrical vessel 11 which is located in a Dewar vessel 12 containing a freezing mixture having a temperature of -80 C, thus freezing out water and ethanol. Carbon dioxide is withdrawn from cylindrical vessel 11 via a line 13 and conducted via a valve 14 which, in this experiment, is open, a line 15, a line 16 and a gas circulation pump 17 into the line 5.The pressure in line 5 is 1.1 bar.
Table 1 hereinafter shows the composition of the liquid present in the fermentation tower 1, of the gas present in the line 7 and of the material frozen out in the vessel 11. Table 1 also shows the heat that has to be added to the fermentation tower 1; expressed in kJ per kg eth-anült TABLE 1
Example Comparative Fermentation Line 7, % mol Vessel 11, %wt Vessel 26, %wt Heat of
Experiment tower 1, %wt evaporation
KJ/kg ethanol
H2O ethanol CO2 H2O ethanol H2O ethanol H2O ethanol
A 95 5 75.5 19.7 4.8 63 37 - - 4689
B 90 10 72.7 19.2 8.1 48 52 - - 2930 1 95 5 75.5 19.7 4.8 - - 43.2 56.8 2562 2 90 10 72.7 19.2 8.1 - - 26.5 73.5 1662 Examples 1 and 2
Examples 1 and 2 are carried out as described in Comparative
Experiments A and B, respectively, with the exception that the valves 9 and 14 are closed.The gas conducted through the line 7 is passed via a line 18 through a valve 19 which, in these examples, is open and through a line 20 into a retentate zone 21 in which it is brought into contact with a selectively permeable membrane 22 that is selectively permeable to ethanol and substantially impermeable to carbon dioxide and water. The membrane 22 has a membrane surface of 100 cm2 and a flux of 0.84 kg per m2 per day.
It consists of 65% by weight of silicalite (manufactured according to US patent specification 4,061,724) in polydimethylsiloxane and has a thickness of 100 pm. The silicalite has a particle size of 1 m and the membrane has a selectivity a of 25. The membrane 22 splits the gas into two gases: a gas substantially consisting of ethanol and water and withdrawn from a permeate zone 23 via a line 24 and a gas substantially consisting of carbon dioxide and water and withdrawn from the retentate zone 21 via a line 25. The line 24 extends into a cylindrical vessel 26 which is located in a
Dewar vessel 27.containing a freezing mixture having a temperature of -80 C, thus freezing out water and ethanol. Residual amounts of carbon dioxide are withdrawn from the cylindrical vessel 26 via a line 28 and a vacuum pump 29 and disposed of via a line 30.
The gas withdrawn from the retentate zone 21 via the line 25 is introduced into the line 16, the valve 14 being closed. Make-up carbon dioxide is supplied via a line 31 into the line 25.
Table 1 hereinbefore shows the composition of the liquid present in the fermentation tower 1, of the gas present in the of the material condensed in the vessel 26. Table 1 also shows the heat that has to be added to the fermentation tower 1, expressed in kJ per kg ethanol.
Comparison between Comparative Experiment A and Example 1 shows that the heat of evaporation -ln Example 1 is. 45% lower.
Comparison between Comparative Experiment B and Example 2 shows that che heat of evaporation in xample 2 is 43% lower.
Both values are considerably lower because a substantial portion of the water remains in vapour form in line 25 and can be recirculated as such to the fermentation tower 1.
Claims (11)
1. A process for the recovery of a volatile organic compound from a biomass containing said volatile organic compound and water and in which biomass said volatile organic compound has been produced by fermentation of fermentable organic compounds by a fermenting agent, which process comprises stripping said biomass with a stripping gas, withdrawing a gaseous mixture comprising stripping gas, volatile organic compound and water from the biomass, contacting said withdrawn gaseous mixture with the upstream side of a membrane which is selectively permeable to said volatile organic compound and recovering a permeate comprising said volatile organic compound from the downstream side of the membrane.
2. A process as claimed in claim 1 in which the membrane comprises a matrix in which an absorbent is present that selectively absorbs said volatile organic compound.
3. A process as claimed in claim 2 in which the absorbent is a silicalite as defined hereinbefore.
4. A process as claimed in claim 2 or 3 in which the matrix comprises poly(dimethyl siloxane).
5. A process as claimed in any one of the preceding claims in which retentate recovered from the upstream side of the membrane is used for stripping said biomass.
6. A process as claimed in any one of the preceding claims in which the volatile organic compound is ethanol.
7. A process as claimed in any one of the preceding claims in which the stripping gas comprises carbon dioxide.
8. A process as claimed in any one of the preceding claims in which the membrane has a thickness in the range of from 0.1 to 200 micrometre.
9. A process as claimed in any one of the preceding claims in which the volatile organic compound is recovered from the permeate by condensation thereof and contacting the condensate with the upstream side of a pervaporation membrane which is selectively permeable to water vapour, recovering liquid volatile organic compound from the upstream side of the pervaporation membrane and withdrawing water vapour from the downstream side of the pervaporation membrane.
10. A process as claimed in claim 1 substantially as hereinbefore described with reference to Examples 1 and 2.
11. Volatile organic compounds whenever recovered by a process as claimed in any one of the preceding claims.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB8703984A GB2201413A (en) | 1987-02-20 | 1987-02-20 | Recovery of volatile organic compounds from a biomass |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB8703984A GB2201413A (en) | 1987-02-20 | 1987-02-20 | Recovery of volatile organic compounds from a biomass |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| GB8703984D0 GB8703984D0 (en) | 1987-03-25 |
| GB2201413A true GB2201413A (en) | 1988-09-01 |
Family
ID=10612638
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB8703984A Withdrawn GB2201413A (en) | 1987-02-20 | 1987-02-20 | Recovery of volatile organic compounds from a biomass |
Country Status (1)
| Country | Link |
|---|---|
| GB (1) | GB2201413A (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0373538A1 (en) * | 1988-12-16 | 1990-06-20 | Kali-Chemie Aktiengesellschaft | Process for the separation of alcohol/water mixtures |
| US5302750A (en) * | 1993-05-25 | 1994-04-12 | Exxon Chemical Patents Inc. | Method for producing n-octadienol from butadiene |
| EP0695210A4 (en) * | 1993-04-19 | 1996-05-01 | Envirosep Inc | Thick film equilibrium process and device |
| GB2324257A (en) * | 1997-04-14 | 1998-10-21 | Univ East London | Pervaporation of ethanol/water mixtures |
| US5868906A (en) * | 1995-05-15 | 1999-02-09 | Athens Corporation | Dehydration and purification of isopropyl alcohol to an ultradry and ultrapure level |
| WO2013173562A1 (en) * | 2012-05-17 | 2013-11-21 | Shell Oil Company | Process for producing volatile organic compounds from biomass material |
| US9206357B2 (en) | 2012-05-17 | 2015-12-08 | Shell Oil Company | Methods and systems for processing biomass material |
-
1987
- 1987-02-20 GB GB8703984A patent/GB2201413A/en not_active Withdrawn
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0373538A1 (en) * | 1988-12-16 | 1990-06-20 | Kali-Chemie Aktiengesellschaft | Process for the separation of alcohol/water mixtures |
| EP0695210A4 (en) * | 1993-04-19 | 1996-05-01 | Envirosep Inc | Thick film equilibrium process and device |
| US5302750A (en) * | 1993-05-25 | 1994-04-12 | Exxon Chemical Patents Inc. | Method for producing n-octadienol from butadiene |
| US5868906A (en) * | 1995-05-15 | 1999-02-09 | Athens Corporation | Dehydration and purification of isopropyl alcohol to an ultradry and ultrapure level |
| GB2324257A (en) * | 1997-04-14 | 1998-10-21 | Univ East London | Pervaporation of ethanol/water mixtures |
| WO2013173562A1 (en) * | 2012-05-17 | 2013-11-21 | Shell Oil Company | Process for producing volatile organic compounds from biomass material |
| US8946491B2 (en) | 2012-05-17 | 2015-02-03 | Shell Oil Company | Process for producing volatile organic compounds from biomass material |
| US9206357B2 (en) | 2012-05-17 | 2015-12-08 | Shell Oil Company | Methods and systems for processing biomass material |
| US9242915B2 (en) | 2012-05-17 | 2016-01-26 | Shell Oil Company | Process for producing volatile organic compounds from biomass material |
| US9359557B2 (en) | 2012-05-17 | 2016-06-07 | Shell Oil Company | Process for producing volatile organic compounds from biomass material |
| US9624436B2 (en) | 2012-05-17 | 2017-04-18 | Shell Oil Company | Methods and systems for processing biomass material |
Also Published As
| Publication number | Publication date |
|---|---|
| GB8703984D0 (en) | 1987-03-25 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| WAP | Application withdrawn, taken to be withdrawn or refused ** after publication under section 16(1) |