CN109294893B - Resource utilization system and method for white spirit brewing byproduct yellow water - Google Patents
Resource utilization system and method for white spirit brewing byproduct yellow water Download PDFInfo
- Publication number
- CN109294893B CN109294893B CN201811278325.0A CN201811278325A CN109294893B CN 109294893 B CN109294893 B CN 109294893B CN 201811278325 A CN201811278325 A CN 201811278325A CN 109294893 B CN109294893 B CN 109294893B
- Authority
- CN
- China
- Prior art keywords
- chamber
- alkali
- lactic acid
- acid
- yellow 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.)
- Active
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 123
- 238000000034 method Methods 0.000 title claims abstract description 52
- 239000006227 byproduct Substances 0.000 title claims abstract description 19
- JVTAAEKCZFNVCJ-UHFFFAOYSA-N lactic acid Chemical compound CC(O)C(O)=O JVTAAEKCZFNVCJ-UHFFFAOYSA-N 0.000 claims abstract description 230
- 239000004310 lactic acid Substances 0.000 claims abstract description 115
- 235000014655 lactic acid Nutrition 0.000 claims abstract description 115
- 238000000855 fermentation Methods 0.000 claims abstract description 90
- 230000004151 fermentation Effects 0.000 claims abstract description 83
- 239000002253 acid Substances 0.000 claims abstract description 65
- 239000012528 membrane Substances 0.000 claims abstract description 41
- 150000003839 salts Chemical class 0.000 claims abstract description 32
- 238000000605 extraction Methods 0.000 claims abstract description 29
- 238000000909 electrodialysis Methods 0.000 claims abstract description 27
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 24
- 238000000926 separation method Methods 0.000 claims abstract description 20
- 239000006228 supernatant Substances 0.000 claims abstract description 7
- 239000003011 anion exchange membrane Substances 0.000 claims abstract description 4
- 238000005341 cation exchange Methods 0.000 claims abstract description 4
- 239000003513 alkali Substances 0.000 claims description 80
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 35
- 238000003860 storage Methods 0.000 claims description 33
- 238000004064 recycling Methods 0.000 claims description 24
- 239000000796 flavoring agent Substances 0.000 claims description 17
- 235000019634 flavors Nutrition 0.000 claims description 16
- 239000000126 substance Substances 0.000 claims description 16
- 239000000047 product Substances 0.000 claims description 13
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 12
- 150000002148 esters Chemical class 0.000 claims description 11
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 10
- 239000002585 base Substances 0.000 claims description 10
- 150000007524 organic acids Chemical class 0.000 claims description 8
- 241000186660 Lactobacillus Species 0.000 claims description 7
- 229940039696 lactobacillus Drugs 0.000 claims description 7
- 239000001569 carbon dioxide Substances 0.000 claims description 6
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 6
- 238000002425 crystallisation Methods 0.000 claims description 6
- 230000008025 crystallization Effects 0.000 claims description 6
- 238000001914 filtration Methods 0.000 claims description 6
- 102000004190 Enzymes Human genes 0.000 claims description 5
- 108090000790 Enzymes Proteins 0.000 claims description 5
- 239000000284 extract Substances 0.000 claims description 5
- 241000894006 Bacteria Species 0.000 claims description 4
- 230000005684 electric field Effects 0.000 claims description 4
- 238000010992 reflux Methods 0.000 claims description 3
- 239000012141 concentrate Substances 0.000 claims description 2
- 208000021302 gastroesophageal reflux disease Diseases 0.000 claims description 2
- 125000002485 formyl group Chemical class [H]C(*)=O 0.000 claims 3
- CYDQOEWLBCCFJZ-UHFFFAOYSA-N 4-(4-fluorophenyl)oxane-4-carboxylic acid Chemical compound C=1C=C(F)C=CC=1C1(C(=O)O)CCOCC1 CYDQOEWLBCCFJZ-UHFFFAOYSA-N 0.000 claims 2
- 239000001540 sodium lactate Substances 0.000 claims 2
- 229940005581 sodium lactate Drugs 0.000 claims 2
- 235000011088 sodium lactate Nutrition 0.000 claims 2
- 235000000346 sugar Nutrition 0.000 abstract description 19
- 239000007788 liquid Substances 0.000 abstract description 17
- 229920002472 Starch Polymers 0.000 abstract description 11
- 235000019698 starch Nutrition 0.000 abstract description 11
- 239000008107 starch Substances 0.000 abstract description 11
- 238000011084 recovery Methods 0.000 abstract description 10
- 239000002699 waste material Substances 0.000 abstract description 10
- 230000007613 environmental effect Effects 0.000 abstract description 5
- 230000008901 benefit Effects 0.000 abstract description 4
- 238000000746 purification Methods 0.000 abstract description 2
- 230000008569 process Effects 0.000 description 20
- 150000001299 aldehydes Chemical class 0.000 description 8
- 238000005265 energy consumption Methods 0.000 description 8
- 159000000007 calcium salts Chemical class 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 7
- 238000004821 distillation Methods 0.000 description 7
- 239000000243 solution Substances 0.000 description 7
- LZCLXQDLBQLTDK-UHFFFAOYSA-N ethyl 2-hydroxypropanoate Chemical compound CCOC(=O)C(C)O LZCLXQDLBQLTDK-UHFFFAOYSA-N 0.000 description 6
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 5
- 239000003456 ion exchange resin Substances 0.000 description 5
- 229920003303 ion-exchange polymer Polymers 0.000 description 5
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 4
- 239000008367 deionised water Substances 0.000 description 4
- 229910021641 deionized water Inorganic materials 0.000 description 4
- 229940079919 digestives enzyme preparation Drugs 0.000 description 4
- 239000008103 glucose Substances 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 230000009471 action Effects 0.000 description 3
- 125000003118 aryl group Chemical group 0.000 description 3
- 230000008878 coupling Effects 0.000 description 3
- 238000010168 coupling process Methods 0.000 description 3
- 238000005859 coupling reaction Methods 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 229940088598 enzyme Drugs 0.000 description 3
- 229940116333 ethyl lactate Drugs 0.000 description 3
- 239000011368 organic material Substances 0.000 description 3
- 102000004169 proteins and genes Human genes 0.000 description 3
- 108090000623 proteins and genes Proteins 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- 150000008163 sugars Chemical class 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 230000001580 bacterial effect Effects 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 238000004364 calculation method Methods 0.000 description 2
- 150000001720 carbohydrates Chemical class 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- SHZIWNPUGXLXDT-UHFFFAOYSA-N ethyl hexanoate Chemical compound CCCCCC(=O)OCC SHZIWNPUGXLXDT-UHFFFAOYSA-N 0.000 description 2
- FUZZWVXGSFPDMH-UHFFFAOYSA-N hexanoic acid Chemical compound CCCCCC(O)=O FUZZWVXGSFPDMH-UHFFFAOYSA-N 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 238000005342 ion exchange Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 239000004278 EU approved seasoning Substances 0.000 description 1
- 241000227425 Pieris rapae crucivora Species 0.000 description 1
- 239000008156 Ringer's lactate solution Substances 0.000 description 1
- 241001052560 Thallis Species 0.000 description 1
- 230000002159 abnormal effect Effects 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- MKJXYGKVIBWPFZ-UHFFFAOYSA-L calcium lactate Chemical compound [Ca+2].CC(O)C([O-])=O.CC(O)C([O-])=O MKJXYGKVIBWPFZ-UHFFFAOYSA-L 0.000 description 1
- 239000001527 calcium lactate Substances 0.000 description 1
- 229960002401 calcium lactate Drugs 0.000 description 1
- 235000011086 calcium lactate Nutrition 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 238000012258 culturing Methods 0.000 description 1
- 230000003831 deregulation Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000010494 dissociation reaction Methods 0.000 description 1
- 230000005593 dissociations Effects 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 239000003480 eluent Substances 0.000 description 1
- 238000010828 elution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000032050 esterification Effects 0.000 description 1
- 238000005886 esterification reaction Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 235000013355 food flavoring agent Nutrition 0.000 description 1
- 235000011194 food seasoning agent Nutrition 0.000 description 1
- 238000003306 harvesting Methods 0.000 description 1
- 235000020256 human milk Nutrition 0.000 description 1
- 210000004251 human milk Anatomy 0.000 description 1
- 239000003864 humus Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 238000009533 lab test Methods 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 125000000896 monocarboxylic acid group Chemical group 0.000 description 1
- 235000005985 organic acids Nutrition 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 238000003836 solid-state method Methods 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 238000003815 supercritical carbon dioxide extraction Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 235000020097 white wine Nutrition 0.000 description 1
- 235000014101 wine Nutrition 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
- C12M41/26—Means for regulation, monitoring, measurement or control, e.g. flow regulation of pH
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
- C12M47/10—Separation or concentration of fermentation products
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P7/00—Preparation of oxygen-containing organic compounds
- C12P7/40—Preparation of oxygen-containing organic compounds containing a carboxyl group including Peroxycarboxylic acids
- C12P7/56—Lactic acid
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/26—Treatment of water, waste water, or sewage by extraction
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
- C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/32—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters
- C02F2103/325—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters from processes relating to the production of wine products
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/54—Improvements relating to the production of bulk chemicals using solvents, e.g. supercritical solvents or ionic liquids
Abstract
The invention provides a resource utilization system and a resource utilization method of white spirit brewing byproduct yellow water, wherein the system comprises the following steps: yellow water lactic acid fermentation unit, bipolar membrane electrodialysis unit and supercritical CO 2 An extraction unit; the yellow water lactic acid fermentation unit comprises a fermentation tank, wherein the fermentation tank is connected with an ultrafiltration device, and a supernatant pipeline of the ultrafiltration device is connected with the bipolar membrane electrodialysis unit; the bipolar membrane electrodialysis unit comprises a salt chamber, an acid chamber and a base chamber, wherein the acid chamber and the salt chamber are separated by an anion exchange membrane, the salt chamber and the base chamber are separated by a cation exchange membrane, and the salt chamber is connected with the supercritical CO 2 An extraction unit; the supercritical CO 2 The extraction unit comprises a rectifying tower, and the top of the rectifying tower is connected with a separator. According to the method provided by the invention, starch and reducing sugar in yellow water are fully utilized and converted into lactic acid with higher utilization value; the recovery rate of the lactic acid is high, the lactic acid separation and purification process has no resource consumption and waste liquid discharge, and the environmental benefit is high.
Description
Technical Field
The invention belongs to the technical field of fermentation, and particularly relates to a utilization method and a utilization system of yellow water generated by white spirit fermentation.
Background
Yellow water is a brown yellow fluid liquid deposited at the bottom of a pit because part of water exudes due to the catabolism of the fermented grains by microorganisms in the process of brewing and producing white spirit by a solid state method. Generally, about 300-400 kg of yellow water is produced per 1000kg of white spirit, and the yield of the strong aromatic white spirit in 2017 is 985.5 ten thousand tons, so that the emission of yellow water per year is about 340 ten thousand tons. According to the conventional physicochemical properties of yellow water, the COD of the yellow water is in the range of 135g/L to 330g/L, which is far more than the national allowable wastewater discharge standard. Even through anaerobic-aerobic treatment, the waste water is difficult to reach the standard for discharge. And part of yellow water of winery is directly discharged into water body without treatment, so that the pollution is serious. Therefore, the method for fully recycling the organic matter resources in the yellow water is significant for reducing the sewage treatment load and reducing the environmental pollution.
At present, most wineries in China treat yellow water by adopting methods of vinasse mixing and pit returning fermentation or pit raising, artificial pit mud culturing, bottom returning pot distillation and the like. The method can not only effectively utilize resources and fully reduce COD discharge of the yellow water, but also can not fundamentally solve the problem of optimal comprehensive utilization of the fermented yellow water. Therefore, how to comprehensively utilize the yellow water resource thoroughly solves the problem of optimal comprehensive utilization of the yellow water, and becomes a great subject faced by the white spirit industry. At present, most of the recycling of starch and reducing sugar in yellow water is carried out through ultrafiltration membrane filtration together with thalli and protein to process liquid protein feed, and the utilization rate of starch and reducing sugar is low although COD of yellow water is greatly reduced. The traditional method for extracting flavor substances is a multi-stage distillation method; according to the difference of boiling points of all components in flavor substances in yellow water, carrying out multistage distillation extraction to obtain extracts with different boiling points; in the industrial production process, the energy consumption in the distillation process is high and the distillation efficiency is low due to the large yellow water quantity. The preparation of biological esterified liquid is more studied on enzyme preparations, but the enzyme preparations used by the existing yellow water biological esterified liquid are mostly coarse enzyme preparations, the dosage is large, the esterification effect is poor, and the novel efficient enzyme preparations are still studied at the level of experimental laboratory tests, and industrial production is not seen. At present, the strong aromatic white spirit has the common problem that the content of lactic acid and ethyl lactate in the white spirit is higher than that of caproic acid and ethyl caproate, so that the taste of the white spirit body is poor; the content of lactic acid in the yellow water can be 90% of the total organic acid content, and meanwhile, the lactic acid has great utilization value; if the yellow water does not extract lactic acid before extracting the flavor substances, the content of lactic acid and ethyl lactate in the prepared liquor is very high, and the effect of blending the strong aromatic white spirit is poor.
The existing yellow water is subjected to reducing sugar fermentation by using a calcium salt method to produce the yellow water fermentation liquor after lactic acid is separated, and then flavor substances are extracted, wherein the recovery rate of the calcium salt method to the lactic acid in the yellow water fermentation liquor is only 50%, and a large amount of resources are required to be continuously consumed and a large amount of waste liquid is required to be discharged in the process; other yellow Shui Zhihua liquid preparation methods, namely yellow water byproducts are comprehensively utilized, but environmental resources and safety are sacrificed. And meanwhile, many winery researches on recycling of yellow water are mostly carried out by extracting flavor substances in the yellow water to prepare liquor, seasonings and esterifying the yellow water to prepare esterified liquor for distillation of wine. Firstly, organic materials such as starch and reducing sugar in the yellow water are not fully utilized, and the COD discharge amount of the yellow water is still high; secondly, most of the processes for extracting flavor substances in yellow water are multistage distillation, and the process has low extraction rate of the flavor substances and high energy consumption.
Disclosure of Invention
In order to solve the problems of insufficient recycling of organic materials in the yellow water, high resource consumption, high energy consumption and high discharge of waste liquid and waste residues in the resource recycling process, the invention provides a recycling system of the yellow water which is a byproduct of white spirit brewing, which is used for recycling the yellow waterFermenting the reducing sugar in water to produce lactic acid, and simultaneously separating and extracting the lactic acid by coupling a bipolar membrane electrodialysis process (EDBM); supercritical CO is carried out on the yellow water fermentation liquor after lactic acid separation 2 Extracting to obtain flavoring agent such as alcohol, residual acid, ester and aldehyde.
The invention further aims to provide a resource utilization method of yellow water which is a byproduct of white spirit brewing.
The technical scheme for realizing the purposes of the invention is as follows:
a recycling system of byproduct yellow water in white spirit brewing comprises: yellow water lactic acid fermentation unit, bipolar membrane electrodialysis unit and supercritical CO 2 An extraction unit;
the yellow water lactic acid fermentation unit comprises a fermentation tank, the fermentation tank is connected with an ultrafiltration device, a supernatant pipe of the ultrafiltration device is connected with the bipolar membrane electrodialysis unit, and a concentrated solution outlet of the ultrafiltration device is connected with the fermentation tank through a circulating pipe.
The bipolar membrane electrodialysis unit comprises a salt chamber, an acid chamber and a base chamber, wherein the acid chamber and the salt chamber are separated by an anion exchange membrane, the salt chamber and the base chamber are separated by a cation exchange membrane, the acid chamber and the base chamber are separated by a bipolar membrane (the salt chamber is positioned between the acid chamber and the base chamber), and the salt chamber is connected with the supercritical CO 2 An extraction unit;
the supercritical CO 2 The extraction unit comprises a rectifying tower, and the top of the rectifying tower is connected with a separator.
Preferably, the concentrate outlet of the ultrafiltration device is connected to the fermenter via a circulation line. And a fermentation controller is arranged on the fermentation tank. Wherein the bipolar membrane electrodialysis units are 2-100 repeated units, and the units are arranged in parallel.
The invention has the following optional scheme: the membrane stack specification was 800mm×400mm, and the number of unit repetitions per 1000L (treated water amount) was 5 groups.
Wherein the alkali chamber is connected with an alkali storage tank through an alkali outlet pipeline, and the alkali storage tank is connected with the fermentation tank; more preferably, the alkali storage tank is connected to the alkali chamber by an alkali return line.
The acid chamber is connected with a lactic acid storage tank through an acid outlet pipeline, and the lactic acid storage tank is connected with a concentration crystallization device; preferably, the lactic acid tank is connected to the acid chamber by a lactic acid return line.
Wherein the supercritical CO 2 The extraction unit comprises a rectifying tower, and the top of the rectifying tower is connected with a first separator and a second separator.
A resource utilization method of white spirit brewing byproduct yellow water comprises the following steps:
1) Adding saccharifying enzyme and lactobacillus into yellow water into a fermentation tank for anaerobic fermentation, and filtering fermentation liquor by an ultrafiltration device after fermentation is completed to remove thallus residues;
2) Supernatant separated by the ultrafiltration device enters a salt chamber of a bipolar membrane electrodialysis unit, and HLa is carried out under the action of an external electric field - Transferring the lactic acid into an acid chamber, and when the concentration of the acid chamber reaches 60-85% of the concentration of a salt chamber, separating to obtain lactic acid, storing the lactic acid in an acid storage tank, and concentrating and crystallizing to obtain a lactic acid finished product; OH (OH) - Entering an alkali chamber, and when the concentration of the alkali chamber reaches 60-85% of the concentration of the salt chamber, separating alkali liquor and storing the alkali liquor in an alkali storage tank (after which deionized water is added in a supplementary way);
3) And the salt chamber effluent of the bipolar membrane electrodialysis unit is residual yellow water after lactic acid is separated, and the residual yellow water is pumped into a supercritical carbon dioxide rectifying tower to extract flavor substances.
The yellow water contains abundant beneficial microorganisms, the lactobacillus accounts for 15.9 percent, is dominant bacteria, and has the potential of producing lactic acid by fermentation for reducing COD emission of the yellow water.
Lactic acid fermentation is the process by which lactic acid bacteria under anaerobic conditions ferment reduced sugars to lactic acid. Lactic acid fermentation is classified into homolactic fermentation and heterolactic fermentation. In homotype fermentation of lactic acid, 1C 6 H 12 O 6 →2C 3 H 6 O 3 1 molecule of glucose generates 2 molecules of lactic acid, namely 1g of glucose is fermented to generate 1g of lactic acid, and the theoretical conversion rate of glucose is 100%. 1C when lactic acid is subjected to abnormal fermentation 6 H 12 O 6 →1C 3 H 6 O 3 ,1C 2 H 5 OH(or 1.5CH 3 COOH), 1 molecule of glucose produced 1 molecule of lactic acid, with a theoretical conversion of 50%.
However, the main limiting factors for the fermentation of reducing sugars in yellow water to produce lactic acid are yellow water pH and product inhibition. The pH range of the yellow water is 2.8-4.6, and the pH value of the lactobacillus fermentation can be adjusted to be 5-7. Meanwhile, the COD content of the organic acid in the yellow water is about 1/3 of the total COD, wherein the COD content of the lactic acid is 90%, so that the lactic acid with high concentration in the fermentation liquid can inhibit the yellow water from lactic acid fermentation. The yellow Shui Rusuan fermentation coupling EDBM lactic acid separation process adopted by the method can realize in-situ separation fermentation of lactic acid. The high-purity alkali liquor generated by bipolar membrane electrodialysis can be used for regulating the pH constant in the fermentation process, and the conversion rate of lactic acid produced by reducing sugar fermentation is improved.
Further, 90 to 99% of the cells in the concentrated solution obtained by passing the fermentation broth through the ultrafiltration device are recovered, and 1 to 10% of the cells are discharged.
For example, 95% of the cells are recovered and 5% of the cells are discharged.
In the step 1), naOH and/or alkali liquor generated by a bipolar membrane electrodialysis unit is added into a fermentation tank to adjust the pH value of yellow water to 5.8-6.2, and anaerobic fermentation is carried out.
After the lactic acid is introduced into the acid storage tank from the acid chamber and the NaOH is introduced into the alkali storage tank from the alkali chamber, (when the same volume of deionized water is added), the lactic acid separated from the acid chamber partially flows back to the acid chamber, and the alkali separated from the alkali chamber partially flows back to the alkali chamber, so that the concentration in the acid chamber and the alkali chamber is maintained to be not lower than 0.2mol/L.
Wherein in the step 3), the supercritical carbon dioxide rectifying tower is used for extraction, and a separator is used for separating fractions, and the fractions of acid, ester, alcohol and aldehyde are separated. Wherein the first separator controls the separation pressure to be 7-10 MPa, the separation temperature to be 40-50 ℃, and mainly separates ester products; the second separator controls the separation pressure to be 5-6 MPa, the separation temperature to be 30-50 ℃ and separates alcohol, organic acid and aldehyde products.
The main organic pollutants in the yellow water are saccharides (starch and reducing sugar) and fragrant substances similar to the flavor of white wine:organic acids, alcohols, esters, aldehydes. Wherein the sugar, lactic acid and residual flavor substances each account for about 1/3 of COD of yellow water. The recovery of saccharides in yellow water can be converted into lactic acid by fermentation under the action of saccharifying enzyme and lactobacillus; the recovery of lactic acid is separated by bipolar membrane Electrodialysis (EDBM); the recovery of flavor substances depends on supercritical CO of residual yellow water fermentation liquor after lactic acid extraction 2 And (5) extracting and recycling. The organic material in the yellow water is fully recycled, and the COD emission of the yellow water is reduced to the greatest extent.
The system and the method provided by the invention are characterized in that the yellow water is firstly subjected to starch saccharification and reducing sugar fermentation in a fermentation tank, and meanwhile, the lactic acid generated in the yellow water fermentation process is separated by coupling with a bipolar membrane Electrodialysis (EDBM) process; pumping the residual yellow water fermentation liquor into a supercritical carbon dioxide extraction device to extract flavor substances in the residual yellow water fermentation liquor, performing multiple-cycle extraction, preparing an extract liquor into a liquor mixing liquid, and discharging the liquor into a sewage treatment plant; the separated lactic acid can be further purified to prepare a lactic acid finished product. The resource recycling is maximized, the environmental effect is highest, and the method is suitable for medium and large wineries.
The method provided by the invention has the following advantages:
(1) Starch and reducing sugar in the yellow water are fully utilized and converted into lactic acid with higher utilization value;
(2) The recovery rate of the lactic acid is high, the lactic acid separation and purification process has no resource consumption and waste liquid discharge, and the environmental benefit is high;
(3) Harvesting supercritical CO 2 The process is high in extraction rate, the extraction rate of the organic acid is more than 90%, the total extraction of the flavor substances such as alcohol, ester and aldehyde can be basically realized, and the extract can be used as a high-quality liquor. And the content of lactic acid and ethyl lactate in the obtained liquor is no longer the main flavor substance in the liquor, and the liquor has good effect when being used for blending common white spirit with deregulation of the ratio of the breast milk.
Drawings
FIG. 1 is a schematic diagram of a system for recycling yellow water, a byproduct of brewing white spirit.
The corresponding relation between the parts and the numbers in the figure is as follows:
yellow water enters the pipeline 101, the pH value adjusting pipeline 102, the fermentation tank 103, the ultrafiltration device 104, the circulation pipeline 105, the outlet 106 for discharging bacterial residues, the salt chamber 201, the acid chamber 202, the alkali chamber 203, the alkali storage tank 204, the lactic acid storage tank 205, the concentration crystallization device 206, the residual yellow water pipeline 207, the lactic acid reflux pipeline 208, the rectifying tower 301, the first separator 302, the second separator 303, the kettle liquid collector 304 and the waste liquid discharge pipeline 305.
FIG. 2 is a flow chart of the method for recycling yellow water, a byproduct of brewing white spirit, in the invention.
Detailed Description
The technical scheme of the invention is further described in the following specific examples. It will be appreciated by those skilled in the art that the examples are provided for illustration only and are not intended to limit the scope of the present invention.
In the examples, the technical means used are conventional technical means in the art unless otherwise specified.
Example 1:
referring to fig. 1, a system for recycling yellow water, which is a byproduct of brewing white spirit, comprises: yellow water lactic acid fermentation unit, bipolar membrane electrodialysis unit and supercritical CO 2 An extraction unit;
the yellow water lactic acid fermentation unit comprises a fermentation tank 103, wherein a yellow water inlet pipeline 101 and a pH value adjusting pipeline 102 are arranged at the top of the fermentation tank 103, the fermentation tank is connected with an ultrafiltration device 104, and a supernatant pipeline of the ultrafiltration device 104 is connected with the bipolar membrane electrodialysis unit;
the bipolar membrane electrodialysis unit comprises a salt chamber 201, an acid chamber 202 and a base chamber 203, wherein the acid chamber 202 and the salt chamber 201 are separated by an anion exchange membrane (am), the salt chamber 201 and the base chamber 203 are separated by a cation exchange membrane (cm), the acid chamber 202 and the base chamber 203 are separated by a bipolar membrane (bm), and a residual yellow water pipeline 207 at the top of the salt chamber 201 is connected to the supercritical CO 2 An extraction unit;
the repeating units take the form of parallel connections. In the present embodiment, the membrane stack specification is selected from 0.4mx0.8m, and 10 membrane stack assembly groups (the number of unit repetitions) (fig. 1 shows one unit, and is outlined by a dotted line). The membrane stack specification is 800mm×400mm, and the number of unit repetitions per 1000L of the treated water is 5 groups.
The supercritical CO 2 The extraction unit comprises a rectifying tower 301, and a first separator 302 and a second separator 303 are connected to the top of the rectifying tower 301. The rectifying tower kettle is connected with a kettle liquid collector 304. The tank liquid collector 304 is provided with a waste liquid discharge pipe 305.
The concentrated solution outlet of the ultrafiltration device is connected with the fermentation tank 103 through a circulating pipeline 105, and a fermentation controller is arranged on the fermentation tank. The concentrated solution outlet is also connected to an outlet 106 for discharging the bacterial cell residue.
The alkali chamber 203 is connected with an alkali storage tank 204 through an alkali outlet pipeline, and the alkali storage tank is connected with a pH value adjusting pipeline 102 on the fermentation tank; the alkali storage tank is connected with the alkali chamber through an alkali reflux pipeline.
The acid chamber 202 is connected with a lactic acid storage tank 205 through an acid outlet pipeline at the bottom, and the lactic acid storage tank is connected with a concentration crystallization device 206; the lactic acid tank is connected to the acid chamber by a lactic acid return line 208. A lactic acid product outlet is provided at the bottom of the concentrating crystallization device 206.
Example 2
By applying the system of the embodiment 1, a method for recycling yellow water as a byproduct of brewing white spirit, the flow of which is shown in fig. 2, comprises the following operations:
1) Adding saccharifying enzyme and lactobacillus into yellow water after entering a fermentation tank, carrying out anaerobic fermentation, and filtering fermentation liquor by an ultrafiltration device after fermentation is completed; removing macromolecular organic matters such as thallus residues, humus, proteins and the like, and recycling part of thallus in concentrated solution obtained by passing fermentation liquor through an ultrafiltration device into a fermentation tank; specifically, 95% of the cells were recovered and 5% of the cells were discharged. NaOH is added into the fermentation tank during initial operation; and in the operation, the pH value of yellow water is regulated to 6.0 by alkali liquor generated by the bipolar membrane electrodialysis unit, and anaerobic fermentation is carried out.
2) Supernatant separated by the ultrafiltration device enters a salt chamber of a bipolar membrane electrodialysis unit, and HLa is carried out under the action of an external electric field - Transferring into an acid chamber, separating to obtain lactic acid, concentrating and crystallizing to obtain lactic acid finished product; OH (OH) - Enters an alkali chamber and is separated outThe alkali liquor is stored in an alkali storage tank. When the concentration of the acid chamber and the alkali chamber is increased, lactic acid in the acid chamber is respectively led into an acid storage tank, naOH in the alkali chamber is led into an alkali storage tank, then deionized water with the same volume is supplemented, meanwhile, the lactic acid separated from the acid chamber partially flows back to the acid chamber, the alkali separated from the alkali chamber partially flows back to the alkali chamber, and the concentration difference between the salt chamber and the acid chamber and the alkali chamber is maintained to ensure that the concentration in the acid chamber and the alkali chamber is not lower than 0.2mol/L.
3) And the salt chamber effluent of the bipolar membrane electrodialysis unit is residual yellow water after lactic acid is separated, the residual yellow water is pumped into a supercritical carbon dioxide rectifying tower for extracting flavor substances, and the supercritical carbon dioxide rectifying tower is used for extracting, so that fractions of alcohol, acid, ester and aldehyde are separated. In the embodiment, the first separator controls the separation pressure to be 7-10 MPa, the separation temperature is about 40-50 ℃, and the ester products are mainly separated; the second separator controls the separation pressure to be 5-6 MPa, the separation temperature is about 30-50 ℃, and the alcohol, the organic acid and the aldehyde products are separated.
The present example provides a set of yellow water composition data, as shown in Table 1. Table 1 also shows the components after fermentation in the fermenter (Table 1, "yellow water fermentation broth"), the yellow water components discharged from the salt chamber (Table 1, "yellow water fermentation broth after lactic acid extraction"), and the waste water components discharged from the waste liquid discharge line 305.
TABLE 1 Main organic content in each flow in yellow Water resource utilization scheme
In the EDBM process of the present embodiment, the applied current density is 50mA/cm 2 The concentration among the salt chamber, the acid chamber and the alkali chamber is 1.2mol/L of sodium lactate solution in the salt chamber, and each time the concentration of lactic acid in the acid chamber and the concentration of NaOH in the alkali chamber are accumulated to 1.0mol/L, lactic acid is led into the acid storage tank, and NaOH is led into the alkali storage tank; adding the same body into the acid chamber and the alkali chamber respectivelyAnd (3) accumulating deionized water, and simultaneously, refluxing part of lactic acid and NaOH from a lactic acid tank into an acid chamber, so that the concentration of the lactic acid is not lower than 0.2mol/L, and the recovery rate of the lactic acid is 85.4 percent (the recovery rate after bipolar membrane treatment).
The lactic acid content in the raw materials is calculated by 30g/L, the starch content in the yellow water is 40g/L, the reducing sugar content is 50g/L, the starch conversion rate is calculated by 111% of theory, the reducing sugar conversion rate is calculated by 82.7%, the lactic acid separation rate is calculated by 85%, and the residual yellow water is subjected to supercritical CO 2 The extraction rate of the organic acid is 90%, and the extraction rate of the alcohol, the ester and the aldehyde is 95%. After the scheme is utilized, 92kg of lactic acid can be produced by 1t of yellow water, 30kg of liquor is regulated, the COD of the yellow water is reduced by about 96.7%, and the full recycling of organic matters of the yellow water is basically realized.
Example 2
The process conditions of this example were substantially the same as those of example 1, except that the lactic acid content in the yellow water was 40g/L, the starch content was 30g/L, the reducing sugar was 30g/L, and the applied current density was 60mA/cm in the EDBM process 2 The conversion of reducing sugars (lactic acid yield coefficient) was 78.5%; the lactic acid yield during fermentation was 90g/L. The concentration between the acid chamber and the alkali chamber is 73g/L, the concentration of NaOH in the alkali chamber is 32.4g/L, and the recovery rate of lactic acid is 81.22%.
Example 3
The process conditions of this example were substantially the same as in example 1, except that the lactic acid content in the yellow water was 25g/L, the starch content was about 20g/L, the reducing sugar content was about 30g/L, the reducing sugar conversion rate during fermentation was 80%, and the lactic acid yield was 66.76g/L. In EDBM process, the applied current density is 50mA/cm 2 The concentration between the acid chamber and the alkali chamber is 52.3g/L, the concentration of NaOH in the alkali chamber is 23.2g/Lg/L, and the recovery rate of lactic acid is 78.3%.
Comparative example 1
The separation and extraction of lactic acid by ion exchange resin process was carried out, and the raw material was the same as in example 1. The ion exchange resin used was D315 ion exchange resin.
TABLE 2 calculation of lactic acid Material balance by extraction of D315 resin
Note that: in order to obtain molecular lactic acid in industry, no other impurity cations are introduced during the elution process, and H with the mass fraction of 5% is selected 2 SO 4 Preparing eluent; supercritical CO for residual yellow water fermentation liquor 2 No SO is introduced during extraction 4 2- NaOH regeneration solution with mass fraction of 4% is selected.
Comparative example 2
The calcium salt method was used to treat the same starting material as in example 1. Because of the need of concentration crystallization and filtration for multiple times, the lactic acid is lost in each process, and the lactic acid extraction rate is lower than 60 percent. Compared with the calcium salt method and the ion exchange resin method, the EDBM process for extracting lactic acid has the best environmental benefit. Tables 1 and 2 show the resource consumption and waste discharge per 1t of pure lactic acid produced from yellow water by the calcium salt method and the ion exchange method, respectively.
Table 3 calculation of material balance for extracting yellow Shui Rusuan by calcium salt method
Note that: the table does not calculate SO removal during ion exchange 4 2- 、Ca 2+ Acid, alkali and water consumed by the plasma; the amount of the activated carbon is 25% of the amount of the finished product of 80% lactic acid.
In the EDBM technology, under the condition of an external electric field and without the help of external acid and alkali, the bipolar membrane ionizes water into H+ and OH-by an intermediate layer, and the H+ and the OH-enter an acid chamber and an alkali chamber respectively to be combined with La-and Na+ to generate HLa and NaOH. The dissociation of water does not generate any gas, and the energy consumption is low; at the same time, water in the solution continuously enters the middle layer of the bipolar membrane to supplement water consumed by electrolysis. The zero emission of waste is realized in theory. The energy consumption of the EDBM process is lower, and the energy consumption is 0.8-1.2 kW.h. (kgHLa) -1 Range. The ion exchange resin has no energy consumption; the calcium salt method has high energy consumption because a continuous high temperature is required to prevent calcium lactate from crystallizing during the filtration and acidolysis.
The above embodiments are merely illustrative of specific embodiments of the present invention, and not intended to limit the scope of the invention, and those skilled in the art may make various modifications and changes on the basis of the prior art, which should fall within the scope of protection defined in the claims of the present invention.
Claims (7)
1. A recycling system of white spirit brewing byproduct yellow water is characterized by comprising: yellow water lactic acid fermentation unit, bipolar membrane electrodialysis unit and supercritical CO 2 An extraction unit;
the yellow water lactic acid fermentation unit comprises a fermentation tank, wherein the fermentation tank is connected with an ultrafiltration device, a supernatant pipeline of the ultrafiltration device is connected with the bipolar membrane electrodialysis unit, and a concentrated solution outlet of the ultrafiltration device is connected with the fermentation tank through a circulating pipeline; adding saccharifying enzyme and lactobacillus into yellow water into a fermentation tank for anaerobic fermentation, and filtering fermentation liquor by an ultrafiltration device after fermentation is completed to remove thallus residues;
the bipolar membrane electrodialysis unit comprises a salt chamber, an acid chamber and a base chamber, wherein the acid chamber and the salt chamber are separated by an anion exchange membrane, the salt chamber and the base chamber are separated by a cation exchange membrane, the acid chamber and the base chamber are separated by a bipolar membrane, and the salt chamber is connected with the supercritical CO 2 An extraction unit;
the supercritical CO 2 The extraction unit comprises a rectifying tower, and the top of the rectifying tower is connected with a first separator and a second separator; supercritical CO is carried out on the yellow water fermentation liquor after lactic acid separation 2 Extracting, namely extracting alcohol, residual acid, ester and aldehyde in the extract to obtain liquor;
the alkali chamber is connected with an alkali storage tank through an alkali outlet pipeline, and the alkali storage tank is connected with the fermentation tank; the alkali storage tank is connected with the alkali chamber through an alkali reflux pipeline; the acid chamber is connected with a lactic acid storage tank through an acid outlet pipeline, and the lactic acid storage tank is connected with a concentration crystallization device; the lactic acid storage tank is connected with the acid chamber through a lactic acid reflux pipeline;
after lactic acid is introduced from the acid chamber into the lactic acid storage tank and NaOH is introduced from the alkali chamber into the alkali storage tank, a lactic acid portion separated from the acid chamber is refluxed to the acid chamber, and an alkali portion separated from the alkali chamber is refluxed to the alkali chamber, so that the concentration of both lactic acid in the acid chamber and alkali in the alkali chamber is maintained at not less than 0.2mol/L.
2. The recycling system of yellow water as a byproduct of brewing white spirit according to claim 1, wherein the bipolar membrane electrodialysis units are 2-100 repeated units, and each unit is arranged in parallel.
3. The method for recycling the byproduct yellow water in the brewing of the white spirit is characterized by adopting the recycling system as claimed in claim 1 or 2, and comprises the following operations:
1) Adding saccharifying enzyme and lactobacillus into yellow water after entering a fermentation tank, carrying out anaerobic fermentation, and filtering fermentation liquor by an ultrafiltration device after fermentation is completed; the residue of the bacteria is removed and the bacteria are removed,
2) Supernatant separated by the ultrafiltration device enters a salt chamber of a bipolar membrane electrodialysis unit, and La is treated by an external electric field - Transferring the lactic acid into an acid chamber, separating to obtain lactic acid, storing the lactic acid in an acid storage tank, and concentrating and crystallizing to obtain a lactic acid finished product when the concentration of the lactic acid in the acid chamber reaches 60-85% of the concentration of sodium lactate in a salt chamber; OH (OH) - Entering an alkali chamber, and separating alkali liquor and storing the alkali liquor in an alkali storage tank when the alkali concentration in the alkali chamber reaches 60-85% of the sodium lactate concentration in the salt chamber;
3) And the salt chamber effluent of the bipolar membrane electrodialysis unit is residual yellow water after lactic acid is separated, and the residual yellow water is pumped into a supercritical carbon dioxide rectifying tower to extract flavor substances.
4. The method for recycling yellow water, which is a byproduct of brewing white spirit, according to claim 3, wherein 90-99% of the cells are recovered and 1-10% of the cells are discharged from the concentrate obtained by passing the fermentation broth through an ultrafiltration device.
5. The method for recycling yellow water as a byproduct in brewing white spirit according to claim 3, wherein in the step 1), naOH and/or alkali liquor generated by a bipolar membrane electrodialysis unit is added into a fermentation tank to adjust the pH value of the yellow water to 5.8-6.2, and anaerobic fermentation is performed.
6. The method for recycling yellow water, which is a byproduct of brewing white spirit, according to claim 3, wherein after lactic acid is introduced into the acid storage tank from the acid chamber and NaOH is introduced into the alkali storage tank from the alkali chamber, a part of lactic acid separated from the acid chamber flows back to the acid chamber, and a part of alkali separated from the alkali chamber flows back to the alkali chamber, so that the concentration of lactic acid in the acid chamber and the concentration of alkali in the alkali chamber are maintained to be not lower than 0.2mol/L.
7. The method for recycling yellow water as a byproduct in brewing white spirit according to any one of claims 3 to 6, wherein in the step 3), the supercritical carbon dioxide rectifying tower is used for extraction, and a separator is used for separating the fraction, and the fractions of acid, ester, alcohol and aldehyde are separated; wherein the first separator controls the separation pressure to be 7-10 MPa, the separation temperature to be 40-50 ℃, and mainly separates the ester products; the second separator controls the separation pressure to be 5-6 MPa, the separation temperature to be 30-50 ℃, and the alcohol, organic acid and aldehyde products are separated.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811278325.0A CN109294893B (en) | 2018-10-30 | 2018-10-30 | Resource utilization system and method for white spirit brewing byproduct yellow water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811278325.0A CN109294893B (en) | 2018-10-30 | 2018-10-30 | Resource utilization system and method for white spirit brewing byproduct yellow water |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109294893A CN109294893A (en) | 2019-02-01 |
| CN109294893B true CN109294893B (en) | 2024-03-19 |
Family
ID=65145601
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201811278325.0A Active CN109294893B (en) | 2018-10-30 | 2018-10-30 | Resource utilization system and method for white spirit brewing byproduct yellow water |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109294893B (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110643487A (en) * | 2019-09-26 | 2020-01-03 | 南京华创环境技术研究院有限公司 | Fermentation device and system for producing caproic acid by utilizing white spirit brewing byproduct yellow water |
| CN113373182A (en) * | 2021-06-17 | 2021-09-10 | 四川剑南春（集团）有限责任公司 | Method for recovering caproic acid in biological fermentation liquid |
| CN114477579A (en) * | 2022-01-24 | 2022-05-13 | 四川绵竹剑南春酒厂有限公司 | Process for treating waste liquid after production of wine seasoning liquid |
| CN114517142A (en) * | 2022-02-28 | 2022-05-20 | 四川绵竹剑南春酒厂有限公司 | Wine additive preparation process and formula |
| CN114890888A (en) * | 2022-06-20 | 2022-08-12 | 安徽瑞思威尔科技有限公司 | Method for extracting ultrahigh-concentration lactic acid from yellow wine brewing water based on tangential flow membrane technology |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4867997A (en) * | 1985-12-04 | 1989-09-19 | Peter Eckes Kg Mbh | Process for producing alcohol-reduced or alcohol-free beverages made by natural fermentation |
| CN1900263A (en) * | 2006-07-12 | 2007-01-24 | 四川省宜宾五粮液集团有限公司 | Method for extracting wine flavour and fragrance substance from yellow water by super critical CO2 technology |
| CN101392273A (en) * | 2008-11-10 | 2009-03-25 | 南京工业大学 | Clean production process of lactic acid |
| CN105264083A (en) * | 2013-03-08 | 2016-01-20 | 希乐克公司 | Processing biomass |
| CN209243063U (en) * | 2018-10-30 | 2019-08-13 | 北京建筑大学 | A kind of resource utilization system of brewed spirit by-product yellow water |
| CN110627634A (en) * | 2019-08-30 | 2019-12-31 | 安徽省金裕皖酒业有限公司 | Method for separating and extracting lactic acid from daqu liquor by-product yellow water |
| CN110643487A (en) * | 2019-09-26 | 2020-01-03 | 南京华创环境技术研究院有限公司 | Fermentation device and system for producing caproic acid by utilizing white spirit brewing byproduct yellow water |
| CN116640054A (en) * | 2023-02-21 | 2023-08-25 | 北京科技大学 | Method for separating lactic acid from kitchen waste lactic acid fermentation liquid |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8859808B2 (en) * | 2010-08-19 | 2014-10-14 | Paulo Yoshida | Method for obtaining lactic acid with a high degree of purity from fermentative liquor |
| US9915136B2 (en) * | 2016-05-26 | 2018-03-13 | X Development Llc | Hydrocarbon extraction through carbon dioxide production and injection into a hydrocarbon well |
-
2018
- 2018-10-30 CN CN201811278325.0A patent/CN109294893B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4867997A (en) * | 1985-12-04 | 1989-09-19 | Peter Eckes Kg Mbh | Process for producing alcohol-reduced or alcohol-free beverages made by natural fermentation |
| CN1900263A (en) * | 2006-07-12 | 2007-01-24 | 四川省宜宾五粮液集团有限公司 | Method for extracting wine flavour and fragrance substance from yellow water by super critical CO2 technology |
| CN101392273A (en) * | 2008-11-10 | 2009-03-25 | 南京工业大学 | Clean production process of lactic acid |
| CN105264083A (en) * | 2013-03-08 | 2016-01-20 | 希乐克公司 | Processing biomass |
| CN209243063U (en) * | 2018-10-30 | 2019-08-13 | 北京建筑大学 | A kind of resource utilization system of brewed spirit by-product yellow water |
| CN110627634A (en) * | 2019-08-30 | 2019-12-31 | 安徽省金裕皖酒业有限公司 | Method for separating and extracting lactic acid from daqu liquor by-product yellow water |
| CN110643487A (en) * | 2019-09-26 | 2020-01-03 | 南京华创环境技术研究院有限公司 | Fermentation device and system for producing caproic acid by utilizing white spirit brewing byproduct yellow water |
| CN116640054A (en) * | 2023-02-21 | 2023-08-25 | 北京科技大学 | Method for separating lactic acid from kitchen waste lactic acid fermentation liquid |
Non-Patent Citations (2)
| Title |
|---|
| In-situ combination of fermentation and electrodialysis with bipolar membranes for the production of lactic acid: Continuous operation;Xiaolin Wang等;《Bioresource Technology》;第442页第1段，图1 * |
| 黄水生物转化技术研究;周新虎等;《酿酒科技》(第11期);第69页右栏第2-3段、第72页右栏第2段，表5 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109294893A (en) | 2019-02-01 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109294893B (en) | Resource utilization system and method for white spirit brewing byproduct yellow water | |
| CN108103112B (en) | Process for producing fuel ethanol by using corn starch as raw material | |
| Maiorella et al. | Alcohol production and recovery | |
| CN101392273B (en) | Clean production process of lactic acid | |
| CN102732589B (en) | Method for treating threonine mother liquor | |
| CN101648847B (en) | Composite process of fuel alcohol and edible alcohol | |
| CN109574802B (en) | Method for separating 1, 3-propylene glycol, acetic acid and butyric acid from fermentation liquor | |
| JPS6043117B2 (en) | Method for producing volatile organic compounds, especially ethanol, by continuous fermentation | |
| CN1186450C (en) | Method for preparing absolute ethanol by biological substance fermentation and inembrane permeation vaporization | |
| CN101735012B (en) | Method for separating and extracting 2,3-butanediol | |
| CN101648848B (en) | Combined production method for fuel alcohol and edible alcohol | |
| CN101586129A (en) | Method of preparing sodium gluconate from xylose crystallization mother liquor | |
| CN102911854B (en) | Separation and purification device and separation and purification method for butanol and acetone | |
| CN101074258A (en) | Method for separating and extracting phytosterin and Vitamin E from soyabean deodorization distillate | |
| CN102391117B (en) | Method for preparing chlorogenic acid from eucommia leaves | |
| CN209243063U (en) | A kind of resource utilization system of brewed spirit by-product yellow water | |
| WO2023109027A1 (en) | Method for desalting and purifying 1,3-propanediol fermentation broth | |
| CN101165189A (en) | Meso one-step method ethanol production method for potato raw starch | |
| CN101293848B (en) | Glutamic acid extracting technique | |
| CN2910939Y (en) | Ethylalcohol production installation | |
| CN212356909U (en) | Fermented mash evaporation concentration and rectification protein powder co-production system | |
| CN101514155A (en) | Method for separating and extracting pyruvic acid from fermentation broth by an ion exchange method | |
| CN1437864A (en) | Process of making high-concentration waste liquid of aginomoto convert into fodder protein | |
| CN202173793U (en) | Alcohol prefractionator reboiling system using centrifugal clear liquid as cyclic medium | |
| CN101818216B (en) | Method for refining corncob acid hydrolysis solution |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |