CN101830777B - Method for recovering carbon dioxide by salting and extracting dihydric alcohol in fermentation liquor by coupling - Google Patents
Method for recovering carbon dioxide by salting and extracting dihydric alcohol in fermentation liquor by coupling Download PDFInfo
- Publication number
- CN101830777B CN101830777B CN2010103012977A CN201010301297A CN101830777B CN 101830777 B CN101830777 B CN 101830777B CN 2010103012977 A CN2010103012977 A CN 2010103012977A CN 201010301297 A CN201010301297 A CN 201010301297A CN 101830777 B CN101830777 B CN 101830777B
- Authority
- CN
- China
- Prior art keywords
- salt
- extracting
- dihydric alcohol
- fermented liquid
- alcohol
- 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.)
- Expired - Fee Related
Links
- 238000000034 method Methods 0.000 title claims abstract description 49
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 48
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 43
- 230000008878 coupling Effects 0.000 title claims abstract description 9
- 238000010168 coupling process Methods 0.000 title claims abstract description 9
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 9
- 238000000855 fermentation Methods 0.000 title abstract description 20
- 230000004151 fermentation Effects 0.000 title abstract description 20
- 229910002092 carbon dioxide Inorganic materials 0.000 title abstract description 13
- 239000001569 carbon dioxide Substances 0.000 title abstract description 8
- 238000009938 salting Methods 0.000 title abstract 2
- 150000003839 salts Chemical class 0.000 claims abstract description 45
- 238000000926 separation method Methods 0.000 claims abstract description 25
- 239000003960 organic solvent Substances 0.000 claims abstract description 16
- 238000011084 recovery Methods 0.000 claims abstract description 13
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- 150000001447 alkali salts Chemical class 0.000 claims abstract description 3
- 238000002425 crystallisation Methods 0.000 claims abstract description 3
- 230000008025 crystallization Effects 0.000 claims abstract description 3
- 238000001556 precipitation Methods 0.000 claims abstract description 3
- 239000007788 liquid Substances 0.000 claims description 45
- 238000000605 extraction Methods 0.000 claims description 24
- 235000011089 carbon dioxide Nutrition 0.000 claims description 18
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- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 12
- -1 hydrogen salt Chemical class 0.000 claims description 12
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- 239000001257 hydrogen Substances 0.000 claims description 7
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- OWBTYPJTUOEWEK-UHFFFAOYSA-N butane-2,3-diol Chemical compound CC(O)C(C)O OWBTYPJTUOEWEK-UHFFFAOYSA-N 0.000 claims description 4
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- PCHPORCSPXIHLZ-UHFFFAOYSA-N diphenhydramine hydrochloride Chemical compound [Cl-].C=1C=CC=CC=1C(OCC[NH+](C)C)C1=CC=CC=C1 PCHPORCSPXIHLZ-UHFFFAOYSA-N 0.000 description 2
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- 238000005185 salting out Methods 0.000 description 2
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Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
Abstract
The invention belongs to the technical field of bioengineering and relates to a method for recovering carbon dioxide by salting and extracting dihydric alcohol in fermentation liquor by coupling. The method is characterized by comprising the following steps of: adding one or more soluble basic inorganic salts to the fermentation liquor of the dihydric alcohol, and then leading waste gas of an organic solvent to react with the salts to generate a salt phase, wherein CO2 reacts with the salt phase to generate an acid salt with a lower solubility; through a precipitation mode, filtering or centrifugalizing for separating the generated acid salt or adding an organic solvent for solventing out crystallization; renewedly generating a basic salt by utilizing or carrying out pyrolysis on the acid salt which is used as a by-product; and recovering CO2 with a high concentration. The invention solves the problems of complicated separation process, low separation capacity, low total yield, high cost, large CO2 discharge quantity, and the like in the process of separating the dihydric alcohol from the fermentation liquor, has simplified process, short separation time, reduced cost, economy and feasibility and realizes the synchronous recovery of the dihydric alcohol, the inorganic salts and the CO2.
Description
Technical field
The invention belongs to technical field of bioengineering, relate to the stripping technique of microbial fermentation solution and the technique for fixing of carbonic acid gas, specially refer to method and the fermentation and the technique for fixing that separates the carbonic acid gas that is discharged of separation of glycols from fermented liquid.
Background technology
Divalent alcohol has extensive and fine application prospect in industry; As 1; Ammediol and terephthalic acid synthetic new polyester material Zhao polytrimethylene terephthalate (PTT) have the not available good characteristic of many polyester materials, good continuous printing and dyeing property that demonstrates as need not to add any speciality chemical in the tint permanence of recovery of elasticity, uvioresistant, ozone and the oxynitride of nylon appearance, low static, low water absorption, the panchromatic scope and biodegradable etc.2, the 3-butyleneglycol is a kind of valuable liquid fuel, 2, and the 3-butyleneglycol can be used for making important industrial organic solvent methylethylketone; Can also be used to producing the monomeric substance that 2 butylene and 1,3-butadiene etc. are produced synthetic chloroprene rubber; 2 of esterified form, 3-butyleneglycol are the synthetic precursors that gathers imines, can be applicable to medicine, makeup, washing lotion etc.; 2 of the diacetylation form that obtains through catalytic dehydrogenation, the 3-butyleneglycol can be used as the foodstuff additive with high value spices; 2 of levorotatory form, the 3-butyleneglycol is because its lower zero pour can be used as antifreezing agent; In addition, divalent alcohol also demonstrates the potential using value in fields such as dyestuff, explosive, perfume, pharmaceutical carriers, but its expensive price has hindered its widespread use.The fermentative Production divalent alcohol is placed high hopes always, and its industrialized bottleneck is efficient cheap stripping technique exploitation.Recently the emission of carbon-dioxide problem more and more receives publicity, and also will become the important factor of restriction fermentative Production divalent alcohol industrialization.
Because some character of divalent alcohol itself make this purification process very difficult like other impurity of dissolved in high boiling point, high-hydrophilic and the fermented liquid.More extraction separation divalent alcohol from microbial fermentation solution adopts and carries disease germs fermented liquid through high speed centrifugation or through film (like tunica fibrosa) filtering separation cell at present, extracts through extraction, ion exchange resin or methods such as molecular sieve adsorption, underpressure distillation then.Rectifying is the difference of utilizing each component volatilization ability in the mixture; Mixture is constantly separated; But because composition is very complicated in the fermented liquid, before reaching distillation temperature, some soluble parts in the fermented liquid will be condensed into the long-pending piece of thicker oily; Thereby therefore the vaporator rate of the divalent alcohol that slows down should not adopt the method for direct rectifying to extract.To 1, ammediol carries out separate study to Mi-HaeCho etc. with organic extraction method (Process Biochemistry, 2006,41:739 to 744), and used extraction agent is an ETHYLE ACETATE, and separate object is a simulated fermentation broth.Studied extraction process (Tsing-Hua University's journal (natural science edition) to great waves etc.; 2001; 41 (12): 53-55) in dilute solution, separate 1; The process of 3 Ucar 35, result show that common organic extraction (using the chloroform give extraction agent) and complexing abstraction (making complexing agent with tributyl phosphate (TBP), sad, caproic acid etc.) all can not separate 1, ammediol effectively.(Conversion of biomass from agricultureinto useful product s.Final report such as Tsao; USDDE, Contract No, EG-77-S-02-4298; 1978-07-31) find to use in the recyclable fermented liquid of diethyl etherate 75% 2; 3 butyleneglycols, but this method is not suitable for large-scale industrial production because of the solvent usage quantity is only limited to laboratory scale than big and the more high reason of cost.Liu Dehua etc. (CN1634823A) pass through 1 in the aldolization extractive fermentation liquid, ammediol with water-insoluble aldehyde such as butyraldehyde.Reaction, extraction needs the multistep operation, complex process, and operational condition is wayward, and separation efficiency is lower.Because reaction, extraction uses a large amount of aldehyde materials, and its remaining aldehyde can be to 1, the polyreaction that ammediol is participated in has a negative impact, so its industrial prospect allows of no optimist in addition.(Recovery of 2,3butanediol by vacuum membrane distillation.Sep SciTechnol, 1994 such as Qureshi; 29:1733～1748) once in the vacuum membrane distillation process, used a kind of poly tetrafluoroethylene with microvoid structure, this film can allow water vapour to pass through smoothly, but can stop 2; The 3-butyleneglycol passes through, and adopts this method, 2; The final quality concentration of 3-butyleneglycol can be up to 430g/L, but there is big difficulty in later separation.In addition, than higher, the film cost is high, and exists film to pollute, be difficult to problems such as cleaning, is applied so be difficult in the industry to the requirement of equipment for pervaporation, membrane distillation, vacuum membrane distillation.
In the fermentation of divalent alcohol and sepn process, all produce great amount of carbon dioxide, and in current global air temperature warming, each state is making great efforts under the situation about reducing discharging all, the carbon dioxide discharge-reduction of the fermentation industry of divalent alcohol be its following must in the face of and problem of solving.The existing recovery method of carbonic acid gas mainly contains several kinds of pressure swing adsorption process, membrane separation process and absorption processes.Absorption method is to utilize fractionation by adsorption carbonic acid gas such as natural zeolite, molecular sieve, silica gel and gac; But the loading capacity of this method is limited, need be a large amount of sorbent material, adsorption-desorption are frequent, expense is too high; Only be applicable to carbon dioxide absorption (the Xinjiang chemical industry of middle and small scale; 2003, (3): 10214).The film that membrane separation process adopts FM, polyethersulfone usually, gathers peptide, polymeric amide polymeric materialss such as (PI) is processed is according to the permeability contrast of gas with various is come separation of C O
2, but the film pollution causes being difficult to obtain highly purified CO
2(modern chemical industry, 2001,21 (9): 53257).Absorption process is divided into two kinds of physical absorption method and chemical absorption; The former adopts organic cpds such as cold methanol, many glycol ethers, tributyl phosphate and tetramethylene sulfone as lyosorption, and the latter mainly uses ability and CO such as containing salt of wormwood, one-level hydramine (like MEA), secondary hydramine (like DEA, D IPA) and tertiary alcohol amine (like MDEA)
2The solution of reaction absorbs CO earlier as lyosorption
2, the mode through intensification or step-down removes CO then
2, the facility investment that whole process need is higher, more steam or kinetic energy loss.Existing C O
2Immobilization technology mainly comprises biological process, physics method and chemical method.Biological process comprises that apply fertilizer in afforestation, ocean and mikrobe is fixed.Afforestation is effective means, still receives restrictions such as geographical conditions, and ocean fertilising (Yamasaki, 2003) can be accelerated the growth of marine plant, thereby absorbs more CO
2Yet this has also brought more discharge of methane simultaneously, and the latter is proved to be a kind of stronger greenhouse gases.Mikrobe fixedly is that mikrobe is with CO
2For carbon source is translated into organism, microorganism used therefor is divided into two kinds in photosynthetic autotrophs mikrobe and chemosynthetic autotroph mikrobe.The former mainly comprises microalgae and photosynthetic bacterium, and they all contain chlorophyll, is the energy with light; The latter's the energy is mainly derived from H
2, H
2S, S
2O
3 2-, NH
4+, NO
2-, Fe
2+And go back ortho states inorganics etc.Yet this method needs the long time, is processing cost higher, so still be in laboratory stage (Energy Conversion andManagement, 2005,46:403 up to now? 20).The physics method mainly comprises bathypelagic storing method and land aqueous stratum (or waste oil, gas well) storing method, but these two kinds of methods can only delay and can not stop CO up hill and dale
2Enter atmosphere (Journal ofEnvironmental Sciences, 2008,20:14? 7).A kind of approach of chemical method is to utilize CO
2Generate valuable chemical with other substance reaction, for example, CO
2With H
2, CH
4, H
2O, CH
3Are OH etc. through (organic chemistry http://epub.edu.cnki.net/grid2008/brief/SourceJump.aspx such as chemical reaction difference synthesizing methanol, methyl-formiate, methylcarbonates? Acid salt ore and CO
2Between reaction generate stable carbonate, but reaction process is extremely slow, can not directly be used for commercial run.Chemical fixation often needs pure CO
2, and the CO of discharging
2Purity generally has only about 20%, and this just needs expensive separation costs.In sum, present carbon dioxide fixation method is that energy consumption is high, facility investment is big, benefit is low mostly.
Separation and CO with divalent alcohol
2The immobilization coupling joins, and this is that we propose basic imagination of the present invention.The inorganic salt of discovering in early stage can not only form double-aqueous phase system with hydrophilic organic solvent, are used for the divalent alcohol product (CN200710010201.X of direct extractive fermentation liquid; And can promote the organic extraction of hydrophobic organic solvent CN200710010203.9), to divalent alcohol.In fact these two kinds of extracting process all be since the ion in the salts solution especially the strong keying action of negatively charged ion and water molecules cause the hydrogen bond action of divalent alcohol and water molecules to weaken; Even final fracture; Be divided into two mutually thereby order about divalent alcohol with salts solution, promptly so-called salting out.Under the situation of not adding organic solvent, have only the bigger inorganic salt of minority solubleness under condition near saturation concentration, could title product be separated from fermented liquid effectively.After adding organic solvent, salting-out effect is remarkable, has reduced the concentration of salt; Expanded the kind of salt; Further strengthen the organic extraction effect and saltout, improved partition ratio, reduced solvent load; Formed the unique way of salt separation extracting, effectively the divalent alcohol product in the extracting and separating fermented liquid.This extraction system of saltouing is easy to into phase, and phase-splitting is clear, and the extraction phase viscosity is low, and solvent is prone to reclaim, and system is prone to amplify, and running cost is low, therefore is expected to solve the problem of divalent alcohol tunning separation difficulty all the time.But the recovery of inorganic salt is key technical problems of its industrial application in the extracting phase.For alkaline, inorganic salts, the saline solution of high density absorbs the great amount of carbon dioxide that discharges in fixedly divalent alcohol fermentation and the sepn process, can reach the purpose that reclaims inorganic salt, can realize the reduction of discharging target of carbonic acid gas again.This is undoubtedly the useful trial of fermentative Production divalent alcohol energy-saving and emission-reduction.
Summary of the invention
The invention provides a kind of method of extraction of saltouing, can be from fermented liquid separation of glycols, can utilize again under its rich salt to absorb the carbonic acid gas that produces in the production process mutually, realize the synchronous recovery of divalent alcohol, inorganic salt and carbonic acid gas.
Technical scheme of the present invention and step are following:
(1) salt separation extracting: the divalent alcohol fermenation raw liquid can carry out pre-treatment with flocculation, filtration, micro-filtration or centrifugation method; Remove thalline and obtain clear liquid; Also can be without pretreated fermenation raw liquid, or through spissated stoste or clear liquid, wherein the concentration range of divalent alcohol be 30700g/L.In above-mentioned fermented liquid or clear liquid, add one or more solubilities alkalescence inorganic salt, it is solid or dense saline solution that institute adds solubility alkalescence inorganic salt, reaches 10%～100% with the saturation ratio of salt in the salt secondary fermentation liquid; Add organic solvent then and form two-phase system or multiphase system, saliferous fermented liquid and volume of organic solvent ratio are 1: 0.01～1: 10.
Divalent alcohol is 1, ammediol, 2,3-butyleneglycol or 1,2-Ucar 35 etc.; Alkaline, inorganic salts is salt of wormwood, yellow soda ash, sodium phosphate, potassiumphosphate or potassium hydrogenphosphate etc.; Organic solvent is ethanol, propyl alcohol, propyl carbinol, amylalcohol, oleyl alcohol, ETHYLE ACETATE, acetone or ether etc.
The mixed solution of this saliferous fermented liquid and organic solvent is left standstill to phase-splitting, on mutually for being rich in the solvent phase or the extraction phase of divalent alcohol, is rich salt face or extracting phase mutually down.From solvent phase, reclaim solvent with distillation or rectification method, obtain the bullion and the solid salt of divalent alcohol.
The extracting operation mode can be intermittently, also can be successive; Can adopt the mode of multistage or counter-current extraction for the less system of partition ratio.
Extracting operation carries out being lower than under the volatile temperature of solvent.In order to make divalent alcohol be assigned to phase as much as possible, macromole such as albumen, nucleic acid, polysaccharide are retained in down mutually with inorganic salt as far as possible, pH value that can regulation system or in system, add complexing agent.Generally between 3-10, complexing agent can be inorganic salts or organic cpds to pH value scope, like tributyl phosphate (TBP), sad, caproic acid etc.
(2) inorganic salt and CO
2Reclaim: CO with the sepn process discharge will ferment
2Waste gas feeds the rich salt face after the extraction, CO
2Generate the lower hydrogen salt of solubleness with the basic salt reaction, by filtering or spinning, perhaps add the organic solvent dilution crystallization with precipitation mode.Rich salt face can be the extracting phase after the extraction, also can be down mutually through the rich salts solution after evaporation concentration or the dilution, and the saturation ratio of its salt is 10%～100%.The gas that is fed can be the CO that fermenting process is discharged
2Waste gas also can be the coal-fired CO that discharges of sepn process power consumption
2Waste gas, or the CO that discharges in fermentation and the sepn process
2Mix waste gas, its concentration range are 1%-99% (v/v).
The hydrogen salt that is generated can be sodium hydrogencarbonate, saleratus, bicarbonate of ammonia, potassium primary phosphate, SODIUM PHOSPHATE, MONOBASIC or sodium hydrogencarbonate etc.The hydrogen salt that is generated can be used as by product and is used, and also can reclaim the CO of high density through the mode of thermal degradation
2, and reclaim alkaline, inorganic salts.
Effect of the present invention and benefit are to the present invention is directed to the separating technology complicacy that separation of glycols exists from fermented liquid at present, and separating power is little, and overall yield is low; Problems such as cost is high, and CO2 emissions are big provide a kind of extracting dihydric alcohol coupling of from fermented liquid, saltouing to reclaim the method for carbonic acid gas; Overcome many drawbacks that extraction separation divalent alcohol technology exists from microbial fermentation solution at present, made technology be able to simplify, disengaging time is short; Cost reduces, economically feasible.Be in particular in: the salt separation extracting has effect of extracting preferably to the divalent alcohol tunning, has solved the lower problem of traditional extraction agent extraction efficiency; Fermented liquid can be directly handled in the salt separation extracting; Exempted the thalline separating step; And can nucleic acid a large amount of in the fermented liquid, albumen, polysaccharide be removed, solved ultrafiltration removal of impurities power consumption big, need clean film, problems such as residual more divalent alcohol can't reclaim in the thalline liquid concentrator; Utilize rich salt face to absorb the carbonic acid gas that produces in the production process and both can reclaim inorganic salt effectively, can reclaim most carbonic acid gas again, solved salt separation extracting salt and reclaimed a large amount of discharging CO in difficulty and the production process
2Problem.
Embodiment
Be described in detail specific embodiment of the present invention below in conjunction with technical scheme.
Be used to produce 1 in the present embodiment; Ammediol and 2; The bacterial classification of 3-butyleneglycol is Cray Bai Shi bacillus (Klebsiellapneumoniae), respectively available from Chinese common micro-organisms DSMZ (CGMCC2028) and Chinese industrial microbial strains preservation administrative center (CICC10011).Must possess the required nutritive ingredient of microorganism growth in the substratum; Like carbon sources such as glycerine or glucose; Nitrogenous source such as yeast extract or yeast powder; Negatively charged ion such as positively charged ions such as sodium, potassium, ammonia, magnesium, calcium and phosphate radical, sulfate radical, cl ions, and trace elements such as zinc, iron, manganese, copper, cobalt, boron and molybdenum.Fermented liquid adopts Cray Bai Shi bacillus to criticize formula stream glycerol adding respectively or glucose fermentation obtains, and wherein 1, the concentration of ammediol is 53g/L, 2, the concentration of 3-butyleneglycol is 65g/L.
Embodiment 1: in the extractive fermentation liquid of saltouing 1, and ammediol
Using molecular weight cut off is that 5,000 dalton, useful area are 1.5m
2Rhodia ultra-filtration membrane (product of Japanese NIPRO company, model FB-150AGA) handle 1, the ammediol fermented liquid obtains clarifying filtrating.Get 10mL filtrating, add potassiumphosphate, add isopyknic ETHYLE ACETATE again, mix, leave standstill, phase-splitting to saturated.Through gas chromatographic detection, obtain 1, the partition ratio of ammediol is 1.28, the recovery is 56.22%.
Embodiment 2: in the extractive fermentation liquid of saltouing 2, and the 3-butyleneglycol
Using molecular weight cut off is that 5,000 dalton, useful area are 1.5m
2Rhodia ultra-filtration membrane (product of Japanese NIPRO company, model FB-150AGA) handle 2,3-butyleneglycol fermentation liquid obtains clarifying filtrating.Get 10mL filtrating, add salt of wormwood, add isopyknic ether again, mix, leave standstill, phase-splitting to saturated.Through gas chromatographic detection, obtain 2, the partition ratio of 3-butyleneglycol is 8.1, the recovery is 90.27%.
Embodiment 3: salt separation extracting 1, the ammediol coupling absorbs CO
2
Using molecular weight cut off is that 5,000 dalton, useful area are 1.5m
2Rhodia ultra-filtration membrane (product of Japanese NIPRO company, model FB-150AGA) handle 1, the ammediol fermented liquid obtains clarifying filtrating.Get 2L filtrating, add the ethanol of 20% (w/w), add yellow soda ash again, mix, leave standstill, phase-splitting to saturated.Through gas chromatographic detection, obtain 1, the partition ratio of ammediol is 7.97, the recovery is 92.13%.To contain 20%CO
2Waste gas feed 1.251 after the extraction with the speed of 200ml/min and contain in the rich salt face of 370g/l yellow soda ash, keep the stirring of 37 ℃ of constant temperature and 500 rev/mins, the CO in the waste gas
2Absorbed by rich salt face, and generate sodium hydrogencarbonate with the yellow soda ash reaction.Along with CO
2The carrying out of absorption reaction, sodium hydrogencarbonate are precipitated gradually and separate out.Every reaction 12h precipitates with the sodium hydrogencarbonate in the filtration under diminished pressure method removal system.Coreaction 48 hours, the recovery of salt has reached 91%, and the high-recovery of carbonic acid gas is 86%, and total yield surpasses 60%.The sodium hydrogencarbonate that is generated obtains yellow soda ash again 200 ℃ of following thermal degradation, and by-product concentration is at the carbonic acid gas more than 95%.
Claims (4)
1. the extracting dihydric alcohol of from fermented liquid, saltouing also is coupled and reclaims the method for carbonic acid gas; It is characterized in that in the fermented liquid of divalent alcohol, adding one or more solubility alkalescence inorganic salt; The concentration of divalent alcohol is 30-700g/L in the fermented liquid, and the saturation ratio of salt reaches 10%～100%; Add organic solvent then and form two-phase system or multiphase system, saliferous fermented liquid and volume of organic solvent are than being 1:0.01～1:10, and used organic solvent is ethanol, propyl alcohol, propyl carbinol, amylalcohol, oleyl alcohol, ETHYLE ACETATE, acetone or ether; To contain 1%-99% (v/v) CO
2Waste gas feed the rich salt face after the extraction, CO
2Generate the lower hydrogen salt of solubleness with reactant salt; The hydrogen salt that generates passes through precipitation mode by filtration or spinning or adding organic solvent dilution crystallization; Hydrogen salt regenerates basic salt as the by product utilization or through thermal degradation, and reclaims the CO of high density
2Used alkaline, inorganic salts is salt of wormwood, yellow soda ash, is solid or dense saline solution.
2. according to the method for described a kind of from fermented liquid, saltout extracting dihydric alcohol and coupling recovery carbonic acid gas of claim 1, it is characterized in that divalent alcohol wherein is 1, ammediol, 2,3-butyleneglycol or 1,2-Ucar 35; Fermented liquid be without pre-treatment contain thalline fermenation raw liquid, without pre-treatment contain thalline liquid concentrator, remove the clear liquid of thalline or remove the liquid concentrator of thalline.
3. the method for carbonic acid gas is reclaimed in said a kind of from fermented liquid, saltout extracting dihydric alcohol and coupling according to claim 1, it is characterized in that the salt separation extracting be intermittently or successive.
4. according to the method for said a kind of from fermented liquid, saltout extracting dihydric alcohol and coupling recovery carbonic acid gas of claim 1, it is characterized in that absorbing CO
2Rich salt face be phase under the separation after the directly extraction, or through the rich salts solution after evaporation concentration or the dilution, the saturation ratio of its salt is 10%～100%.
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| CN101012152A (en) * | 2007-01-24 | 2007-08-08 | 大连理工大学 | Double aqueous phase extraction method for separating 2,3-dihydroxybutane from fermentation liquor |
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