CN102452702B - Recycling method of condensed water - Google Patents
Recycling method of condensed water Download PDFInfo
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- CN102452702B CN102452702B CN 201010513655 CN201010513655A CN102452702B CN 102452702 B CN102452702 B CN 102452702B CN 201010513655 CN201010513655 CN 201010513655 CN 201010513655 A CN201010513655 A CN 201010513655A CN 102452702 B CN102452702 B CN 102452702B
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 110
- 238000000034 method Methods 0.000 title claims abstract description 67
- 238000004064 recycling Methods 0.000 title abstract description 8
- 239000007788 liquid Substances 0.000 claims abstract description 49
- 239000003957 anion exchange resin Substances 0.000 claims abstract description 43
- 238000000855 fermentation Methods 0.000 claims abstract description 39
- 230000004151 fermentation Effects 0.000 claims abstract description 39
- 238000001704 evaporation Methods 0.000 claims abstract description 17
- 238000004519 manufacturing process Methods 0.000 claims abstract description 15
- 238000004821 distillation Methods 0.000 claims abstract description 7
- 238000009833 condensation Methods 0.000 claims description 76
- 230000005494 condensation Effects 0.000 claims description 76
- 239000011347 resin Substances 0.000 claims description 46
- 229920005989 resin Polymers 0.000 claims description 46
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 42
- NIXOWILDQLNWCW-UHFFFAOYSA-N Acrylic acid Chemical class OC(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 claims description 21
- 150000002500 ions Chemical class 0.000 claims description 18
- 230000008020 evaporation Effects 0.000 claims description 16
- 238000002360 preparation method Methods 0.000 claims description 16
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical group CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims description 15
- JVTAAEKCZFNVCJ-UHFFFAOYSA-M Lactate Chemical compound CC(O)C([O-])=O JVTAAEKCZFNVCJ-UHFFFAOYSA-M 0.000 claims description 7
- -1 lactate ions Chemical class 0.000 abstract description 15
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 abstract description 3
- 239000011550 stock solution Substances 0.000 abstract 2
- 230000009286 beneficial effect Effects 0.000 abstract 1
- 239000002585 base Substances 0.000 description 41
- 239000000243 solution Substances 0.000 description 25
- 240000004808 Saccharomyces cerevisiae Species 0.000 description 21
- 239000000203 mixture Substances 0.000 description 21
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 18
- 238000005342 ion exchange Methods 0.000 description 18
- 235000014680 Saccharomyces cerevisiae Nutrition 0.000 description 14
- 102000004190 Enzymes Human genes 0.000 description 13
- 108090000790 Enzymes Proteins 0.000 description 13
- 230000004913 activation Effects 0.000 description 13
- 230000000694 effects Effects 0.000 description 13
- 229940088598 enzyme Drugs 0.000 description 13
- 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 12
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 12
- 239000008367 deionised water Substances 0.000 description 12
- 239000003456 ion exchange resin Substances 0.000 description 12
- 229920003303 ion-exchange polymer Polymers 0.000 description 12
- 229910021641 deionized water Inorganic materials 0.000 description 11
- 240000008042 Zea mays Species 0.000 description 10
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 10
- 239000012670 alkaline solution Substances 0.000 description 10
- 238000001914 filtration Methods 0.000 description 8
- 235000016383 Zea mays subsp huehuetenangensis Nutrition 0.000 description 7
- 102000004139 alpha-Amylases Human genes 0.000 description 7
- 108090000637 alpha-Amylases Proteins 0.000 description 7
- 229940024171 alpha-amylase Drugs 0.000 description 7
- 230000001332 colony forming effect Effects 0.000 description 7
- 238000011081 inoculation Methods 0.000 description 7
- 235000009973 maize Nutrition 0.000 description 7
- 239000002245 particle Substances 0.000 description 7
- 238000005303 weighing Methods 0.000 description 7
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 6
- 238000002791 soaking Methods 0.000 description 6
- 239000002253 acid Substances 0.000 description 5
- 230000003213 activating effect Effects 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 5
- 238000004128 high performance liquid chromatography Methods 0.000 description 5
- 239000004593 Epoxy Substances 0.000 description 4
- 239000004793 Polystyrene Substances 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 238000011068 loading method Methods 0.000 description 4
- 229920002223 polystyrene Polymers 0.000 description 4
- 239000000758 substrate Substances 0.000 description 4
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 3
- 244000061456 Solanum tuberosum Species 0.000 description 3
- 235000002595 Solanum tuberosum Nutrition 0.000 description 3
- 241000209140 Triticum Species 0.000 description 3
- 235000021307 Triticum Nutrition 0.000 description 3
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 description 3
- 150000001450 anions Chemical group 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 235000005822 corn Nutrition 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 238000012262 fermentative production Methods 0.000 description 3
- XUYPXLNMDZIRQH-LURJTMIESA-N N-acetyl-L-methionine Chemical compound CSCC[C@@H](C(O)=O)NC(C)=O XUYPXLNMDZIRQH-LURJTMIESA-N 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 238000005349 anion exchange Methods 0.000 description 2
- 210000004027 cell Anatomy 0.000 description 2
- 230000010261 cell growth Effects 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000007654 immersion Methods 0.000 description 2
- JVTAAEKCZFNVCJ-UHFFFAOYSA-N lactic acid Chemical compound CC(O)C(O)=O JVTAAEKCZFNVCJ-UHFFFAOYSA-N 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 229930182817 methionine Natural products 0.000 description 2
- KDYFGRWQOYBRFD-UHFFFAOYSA-N succinic acid Chemical compound OC(=O)CCC(O)=O KDYFGRWQOYBRFD-UHFFFAOYSA-N 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 229920002472 Starch Polymers 0.000 description 1
- 230000000274 adsorptive effect Effects 0.000 description 1
- 150000001449 anionic compounds Chemical class 0.000 description 1
- 230000001580 bacterial effect Effects 0.000 description 1
- 238000004113 cell culture Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004587 chromatography analysis Methods 0.000 description 1
- 210000004748 cultured cell Anatomy 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 125000003700 epoxy group Chemical group 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000012010 growth Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 229910001412 inorganic anion Inorganic materials 0.000 description 1
- 239000004310 lactic acid Substances 0.000 description 1
- 235000014655 lactic acid Nutrition 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 229920000647 polyepoxide Polymers 0.000 description 1
- 230000000452 restraining effect Effects 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 239000001384 succinic acid Substances 0.000 description 1
Landscapes
- Preparation Of Compounds By Using Micro-Organisms (AREA)
- Treatment Of Water By Ion Exchange (AREA)
Abstract
The invention provides a recycling method of condensed water, wherein the condensed water is obtained after a fermentation liquid and/or a filtered liquid are/is subjected to distillation or evaporating concentration. The method is characterized by comprising the following steps: contacting the condensed water with anion exchange resin, wherein the contact condition ensures that the contents of acetate ions, lactate ions and succinate ions in the contacted condensed water are respectively less than or equal to 20mg/L; and utilizing the processed condensed water to prepare a fermentation stock solution, where the processed condensed water can replace the existing water used for fermentation stock solution. By utilizing the method provided by the invention, the recycling of the condensed water can be successfully realized, the total quantity of water used in a fermentation process is reduced by 30%, and the environmentally-friendly processing load and the environmentally-friendly processing cost can be greatly reduced; and the method provided by the invention is beneficial to the recycling and efficient clean production of water resources.
Description
Technical field
The present invention relates to a kind of reuse method of water of condensation.
Background technology
The enzyme that fermenting process refers to utilize cultured cells is substrate conversion the process of various useful products, and it is widely used in preparing alcohol fuel, food, medicine and various industrial chemicals.Specifically, fermenting process comprises cell cultures, substrate conversion and the product after the substrate conversion is separated on industrial production and purifying.Need in the said process to relate to fermented liquid or cleaner liquid etc. is distilled and evaporation concentration, the water of condensation that the concentrated vapor condenses that produces obtains generally accounts for more than 60% of water total amount of fermentation, generally contains HCO in this water of condensation
3 -, CO
3 2-, SO
4 2-, Cl
-, PO
4 3-Deng inorganic anion and Na
+, Mg
2+, Fe
2+/ Fe
3+, Ca
2+Deng positively charged ion and organic acid such as acetic acid, lactic acid and Succinic Acid etc.
Because a large amount of water of condensation that produces after the distillation of the process such as fermented liquid and/or cleaner liquid or the evaporation concentration has restraining effect to enzyme activity and the Growth of Cells of fermentation, so above-mentioned water of condensation can not be by direct reuse in the preparation fermenation raw liquid.In addition, above-mentioned water of condensation has higher COD value and BOD value, for example, in the Ethanol Production by Fermentation process, the COD value of water of condensation is 4000-5000mg/ml, the BOD value is 300-500mg/ml, and therefore, the water of condensation that produces in the present fermenting process all must can discharge after protecting anaerobism, aerobic treatment through decyclization.
As mentioned above, the water of condensation that produces in the fermenting process at present there is no method and directly recycles, and has increased the producer's environmental protection treatment load and cost, is unfavorable for recycling and high-efficiency cleaning production of water resources.
Summary of the invention
The defective that can't directly recycle in order to overcome the water of condensation that produces in the present fermenting process the invention provides a kind of recycling condensing water method.
The present inventor finds, the content of the acetate moiety that contains in the water of condensation, lactate and succinic ion is all higher, if with the acetate moiety in the water of condensation, lactate and succinic ionic concn be down to respectively enough low after, water of condensation just can be used as fermentation water reuse, and the not growth of the enzyme activity of stopping fermentation and cell.
On the basis of above-mentioned discovery, the invention provides a kind of reuse method of water of condensation, described water of condensation is the water of condensation that obtains after the fermented liquid of fermenting process generation and/or the distillation of cleaner liquid process or the evaporation concentration, it is characterized in that, the method comprises: this water of condensation is contacted with anionite-exchange resin, the condition of contact will be so that the content of acetate moiety, lactate and succinic ion in the water of condensation after the contact respectively less than or equal to 20 mg/litre, and will be used for preparing fermenation raw liquid with the water of condensation after anionite-exchange resin contact.
By method provided by the invention, can make the water of condensation not enzyme activity of stopping fermentation and the growth of cell, thereby can successfully realize the recycling of water of condensation, therefore can make the water total amount of fermenting process descend more than 30%, and environmental protection treatment load and environmental protection treatment cost are significantly descended, be conducive to the high-efficiency cleaning production with the producer of recycling of water resources.
Embodiment
The reuse method that a kind of water of condensation is provided of the present invention, described water of condensation passes through the water of condensation that obtains after distillation or the evaporation concentration with fermented liquid and/or the cleaner liquid that fermenting process produces, it is characterized in that, the method comprises: this water of condensation is contacted with anionite-exchange resin, the condition of contact will be so that the content of acetate moiety, lactate and succinic ion in the water of condensation after the contact respectively less than or equal to 20 mg/litre, and will be used for preparing fermenation raw liquid with the water of condensation after anionite-exchange resin contact.
According to the present invention, described fermenting process can comprise that various is the process of product with substrate conversion by artificial interpolation enzyme and/or cell, preferably including the feedstock conversion that will contain starch by artificial interpolation enzyme and/or bacterial classification is the process of product, for example, produce the process of ethanol from corn, wheat and potato class by fermentation method; Produce the process of citric acid from corn, wheat and potato class by fermentation method; Produce the process of Methionin from corn, wheat and potato class by fermentation method.
According to the present invention, described fermented liquid refers to the liquid form mixt that obtains after fermentation step is finished; The solid content that described cleaner liquid obtains after referring to and will useless tank liquor filtering is less than or equal to the liquid form mixt of 40 grams per liters; Described useless tank liquor refers to fermented liquid is distilled out the rear last liquid form mixt of target product (such as ethanol).
According to the present invention, described concentrated distillation or the evaporative processes that can comprise that various water-contents in the minimizing fluid carry out as purpose, for example, under normal pressure or decompression, heating fermented liquid, cleaner liquid etc. are to impel its evaporation, and described heating means can be carried out heat exchange for the primary steam that will be concentrated the heating of fluid and boiler.
A preferred embodiment of the invention, described water of condensation are in the Ethanol Production by Fermentation process, the secondary steam water of condensation that the useless tank liquor in the tower reactor obtains through the cleaner liquid evaporation that produces after the press filtration.
According to the present invention, in the water of condensation that the cleaner liquid evaporation that produces in the Ethanol Production by Fermentation process obtains, the content of acetate ion can be the 200-600 mg/litre, and the content of lactate ion can be the 300-700 mg/litre, and the content of succinic ion can be the 110-200 mg/litre.
According to the present invention, the condition that water of condensation contacts with anionite-exchange resin can comprise: the temperature of contact can be 20-60 ℃, is preferably 25-40 ℃; The weight ratio of water of condensation and anionite-exchange resin dry weight is 1: 0.0036-0.0125 is preferably 1: 0.0045-0.0075.
According to the present invention, the mode that water of condensation contacts with anionite-exchange resin can be passed through the anion exchange resin bed layer for making water of condensation, the condition of described contact can also comprise: the volume space velocity of water of condensation can be 1.3-3 hour
-1, be preferably 1.6-2.3 hour
-1
According to the present invention, described anionite-exchange resin can be strongly basic anion exchange resin and/or weak base anion-exchange resin.
According to the present invention, described weak base anion-exchange resin is preferably the acrylic acid series weak base anion-exchange resin, phenolic aldehyde is that weak base anion-exchange resin, epoxy are one or more in weak base anion-exchange resin and the polystyrene weak base anion-exchange resin.
Because the acrylic acid series weak base anion-exchange resin has higher exchange capacity and excellent physical strength, so preferred weak base anion-exchange resin is the acrylic acid series weak base anion-exchange resin.
The present inventor finds that macroporous type acrylic acid series weak base anion-exchange resin is with respect to gel-type acrylic acid series weak base anion-exchange resin, have higher exchange capacity and more excellent physical strength, and for acetate moiety, lactate and succinic ion, has higher adsorptive capacity, so processing of the water of condensation that produces in the more suitable fermenting process, therefore, weak base anion-exchange resin macroporous type acrylic acid series weak base anion-exchange resin more preferably.
The present invention has no particular limits the weak base group exchange capacity of weak base anion-exchange resin, in order to save material consumption, energy consumption and the time in the ion exchange process, the preferred weak base anion-exchange resin with larger weak base group exchange capacity that uses, particularly, the preferred weak base group exchange capacity that uses is more than or equal to the macroporous type acrylic acid series weak base anion-exchange resin of 6.5 mmoles/gram dried resin, and further preferred weak base group exchange capacity is the macroporous type acrylic acid series weak base anion-exchange resin of 6.5-12 mmole/gram dried resin.Need to prove that the weak base group exchange capacity described in the present invention is the numerical value that canonical measure obtains according to GB/T 19861-2005.
According to the present invention, described anionite-exchange resin can be by commercially available, for example, described macroporous type acrylic acid series weakly alkaline can be that the ion exchange resin of D310 to D319 obtains by buying the domestic trade mark, D in the trade mark represents macroporous type, deputy 3 expression weakly alkalines, tertiary 1 expression acrylic acid series, the 4th 0 to 9 expression is in order to distinguish the sequence number (SN) of the differences such as group, linking agent.
A preferred embodiment of the invention, described water of condensation is in the Ethanol Production by Fermentation process, the secondary steam water of condensation that useless tank liquor in the tower reactor obtains through the cleaner liquid evaporation that produces after the press filtration, described weak base anion-exchange resin is macroporous type acrylic acid series weak base anion-exchange resin.Wherein, above-mentioned in the Ethanol Production by Fermentation process, the secondary steam water of condensation that concentrated tower reactor press filtration clear liquid produces is that the primary steam that obtains cleaner liquid and boiler heating after the useless tank liquor after the tower reactor distillation is filtered carries out heat exchange, obtains after the secondary steam that this cleaner liquid evaporation is produced condenses.
According to the present invention, described reuse method can also be included in before water of condensation contacts, anionite-exchange resin is activated, and the method for activation can comprise: at first soaking commercially available resin 2-6 hour with acid solution, is 4-6 with deionized water rinsing to pH value then; And then be 7-9 with resin to the pH value after processing with the washed with de-ionized water alkaline solution behind the aqueous slkali soaking 2-8h.
Described acid solution can be aqueous hydrochloric acid, and the concentration of described acid solution can be the 2-8 % by weight.Alkali in the described alkaline solution can be sodium hydroxide and/or potassium hydroxide, and the concentration of described alkaline solution can be the 2-8 % by weight.With respect to every gram dried resin, the consumption of acid solution can restrain for 2-12, and the consumption of alkaline solution can restrain for 2-12.
With respect to every gram dried resin, the deionized water consumption that cleans acid solution is the 6-10 gram; The deionized water consumption that cleans alkali is the 16-48 gram.
According to the present invention, form the ion exchange resin bed layer in the exchange column of the resin after the activation can being packed into, the method for resin dress post is that those skilled in the art are known, does not repeat them here.
According to the present invention, with water of condensation with after weak base anion-exchange resin contacts, can by chromatography detect with water of condensation after weak base anion-exchange resin contacts in the concentration of organic acid ion, if the concentration of acetate moiety, lactate and succinic ion is less than or equal to respectively 20 mg/litre, then the water of condensation after the contact can be used for the preparation fermenation raw liquid.
Described fermenation raw liquid is the various moisture stock liquid for fermentative production, such as: the farinaceous size in the farinaceous size in the Ethanol Production by Fermentation process, the fermentative Production citric acid process, the farinaceous size in the fermentative Production Methionin process etc.
According to the present invention, described reuse method can also comprise contacting with alkaline solution with weak base anion-exchange resin after water of condensation contacts, regenerate.Identical in the definition of described alkaline solution and the activation step, the mode that weak base anion-exchange resin contacts with alkaline solution can be passed through the weak base anion-exchange resin bed for making alkaline solution, the condition of described contact can comprise: the temperature of contact can be 20-60 ℃, and the volume space velocity of alkaline solution can be 1.3-3 hour
-1, the weight ratio of alkaline solution and weak base anion-exchange resin dry weight can be 1: 0.0036-0.0125.
Need to prove the volume among the present invention under the accurate state of the equal index of the volume of gas and liquid.
Below by embodiment content of the present invention is illustrated particularly, but scope of the present invention should be confined among the embodiment.
Embodiment 1
This embodiment is used for illustrating the reuse method of water of condensation provided by the invention.
(1) preparation of the activation of resin and ion exchange resin bed layer
Soak macroporous type acrylic acid series weakly-basic anion exchange dried resin (the Jiangsu Su Qing engineering of water treatment Group Co.,Ltd of 800 grams with the hydrochloric acid soln of 2L concentration 4 % by weight, resin grade D318, the weak base group exchange capacity is more than or equal to 6.5 mmoles/every gram dried resin), soaking after 4 hours with deionized water rinsing to pH value is between the 4-6.Being the sodium hydroxide solution contact of 5 % by weight after 6 hours with 2L concentration again, is between the 7-9 with water wash to leacheate pH value, the macroporous type acrylic acid series weak base anion-exchange resin after obtaining activating.Loading into diameter with macroporous type acrylic acid series weak base anion-exchange resin 25 grams after the above-mentioned activation is 2.18 centimetres, highly is 110 centimetres ion exchange resin bed layer.
(2) ion-exchange
Making temperature is in 50 ℃ the Ethanol Production by Fermentation process, the secondary steam water of condensation that the cleaner liquid evaporation that produces after the useless tank liquor process press filtration in the tower reactor obtains (wherein, the content of acetate ion is 450 mg/litre, the content of lactate ion is 650 mg/litre, and the content of succinic ion is 180 mg/litre) with 2.3 hours
-1Volume space velocity by above-mentioned ion exchange column, carry out ion-exchange, collect the solution after the exchange.Utilizing the acetate moiety concentration in the solution after the HPLC method records exchange is 5 mg/litre, and the content of lactate ion is less than 0.01 mg/litre, and the content of succinic ion is less than 0.01 mg/litre.
(3) preparation fermenation raw liquid and fermentation
Be that solution after 1500 microns crush maize product and the 220g exchange is mixed to get farinaceous size with the 100g average particle diameter.Under 50 ℃, above-mentioned farinaceous size is mixed with the α-amylase (Novozymes Company buys) of 100,000 enzyme activity units, obtain mixture, regulate the pH value to 5 of mixture, and kept 50 minutes, obtain enzymolysis product; Make the temperature of enzymolysis product be down to 33 ℃, with the weighing scale of every gram enzymolysis product, inoculation 10
5The yeast saccharomyces cerevisiae of colony-forming unit (the super highly active dry yeast in Angel, Hubei Angel Yeast stock company), the gained mixture is treated fermentation ends 33 ℃ of lower cultivations 65 hours, the wine degree that adopts oenometer to record tunning is 14.39 volume %.
Comparative Examples 1
This embodiment is used for explanation without the effect of the water of condensation direct reuse of ion exchange treatment.
Preparation fermenation raw liquid and fermentation
With the 100g average particle diameter be 1500 microns crush maize product and 220g with embodiment 1 in the identical secondary steam water of condensation without ion exchange treatment be mixed to get farinaceous size.Under 50 ℃, above-mentioned farinaceous size is mixed with the α-amylase (Novozymes Company buys) of 100,000 enzyme activity units, obtain mixture, regulate the pH value to 5 of mixture, and kept 50 minutes, obtain enzymolysis product; Make the temperature of enzymolysis product be down to 33 ℃, with the weighing scale of every gram enzymolysis product, inoculation 10
5The yeast saccharomyces cerevisiae of colony-forming unit (the super highly active dry yeast in Angel, Hubei Angel Yeast stock company), the gained mixture is treated fermentation ends 33 ℃ of lower cultivations 65 hours, the wine degree that adopts oenometer to record tunning is 12.71 volume %.
Comparative Examples 2
This embodiment is used for illustrating the ferment effect of fresh deionized water.
Preparation fermenation raw liquid and fermentation
Be that the fresh deionized water of 1500 microns crush maize product and 220g is mixed to get farinaceous size with the 100g average particle diameter.Under 50 ℃, above-mentioned farinaceous size is mixed with the α-amylase (Novozymes Company buys) of 100,000 enzyme activity units, obtain mixture, regulate the pH value to 5 of mixture, and kept 50 minutes, obtain enzymolysis product; Make the temperature of enzymolysis product be down to 33 ℃, with the weighing scale of every gram enzymolysis product, inoculation 10
5The yeast saccharomyces cerevisiae of colony-forming unit (the super highly active dry yeast in Angel, Hubei Angel Yeast stock company), the gained mixture is treated fermentation ends 33 ℃ of lower cultivations 65 hours, the wine degree that adopts oenometer to record tunning is 14.45 volume %.
Embodiment 2
This embodiment is used for illustrating the reuse method of water of condensation provided by the invention.
(1) preparation of the activation of resin and ion exchange resin bed layer
Be gel-type acrylic acid series weakly-basic anions exchange dried resin (the Jiangsu Su Qing that the hydrochloric acid soln of 4 % by weight soaks 800 grams with 2L concentration, resin grade 313, the weak base group exchange capacity is more than or equal to 5.5 mmoles/every gram dried resin), soaking after 4 hours with deionized water rinsing to pH value is between the 4-6, be that the sodium hydroxide solution 2L contact of 5% weight is after 6 hours with concentration again, it is between the 7-9 that water cleans drip washing to leacheate pH value, the gel-type acrylic acid series weak base anion-exchange resin after obtaining activating.Loading into diameter with gel-type acrylic acid series weak base anion-exchange resin 25 grams after the above-mentioned activation is 2.18 centimetres, highly is 106 centimetres ion exchange resin bed layer.
(2) ion-exchange
Make in the Ethanol Production by Fermentation process, the secondary steam water of condensation that the cleaner liquid evaporation that produces after the useless tank liquor process press filtration in the tower reactor obtains (wherein, Determination of Ac is 514 mg/litre, the content of lactate ion is 320 mg/litre, and the content of succinic ion is 150 mg/litre) with 1.6 hours
-1Volume space velocity by above-mentioned ion exchange column, carry out ion-exchange, collect the solution after the exchange.Utilizing the acetate moiety concentration in the solution after the HPLC method records exchange is 7 mg/litre, and the content of lactate ion is 0.1 mg/litre, and the content of succinic ion is 0.1 mg/litre.
(3) preparation fermenation raw liquid and fermentation
Be that solution after 1500 microns crush maize product and the 220g exchange is mixed to get farinaceous size with the 100g average particle diameter.Under 50 ℃, above-mentioned farinaceous size is mixed with the α-amylase (Novozymes Company buys) of 100,000 enzyme activity units, obtain mixture, regulate the pH value to 5 of mixture, and kept 50 minutes, obtain enzymolysis product; Make the temperature of enzymolysis product be down to 33 ℃, with the weighing scale of every gram enzymolysis product, inoculation 10
5The yeast saccharomyces cerevisiae of colony-forming unit (the super highly active dry yeast in Angel, Hubei Angel Yeast stock company), the gained mixture is treated fermentation ends 33 ℃ of lower cultivations 65 hours, the wine degree that adopts oenometer to record tunning is 14.15 volume %.
Embodiment 3
This embodiment is used for illustrating the reuse method of water of condensation provided by the invention.
(1) preparation of the activation of resin and ion exchange resin bed layer
Concentration with 2L is polystyrene weakly-basic anions exchange dried resin (the Jiangsu Su Qing of hydrochloric acid soln immersion 800 grams of 4 % by weight, D306, the weak base group exchange capacity is more than or equal to 4.8 mmoles/every gram dried resin), soak after 4 hours be 4-6 with deionized water rinsing to pH value after, be after the sodium hydroxide solution 2L of 5 % by weight soaks 6 hours with the concentration of 2L again, be 7-9 with water wash to leacheate pH value, the polystyrene weak base anion-exchange resin after obtaining activating.Loading into diameter with polystyrene weak base anion-exchange resin 25 grams after the above-mentioned activation is 2.18 centimetres, highly is 108 centimetres ion exchange resin bed layer.
(2) ion-exchange
Make in the Ethanol Production by Fermentation process, the secondary steam water of condensation (wherein, Determination of Ac is 514 mg/litre, and the content of lactate ion is 481 mg/litre, and the content of succinic ion is 125 mg/litre) that the fermented liquid evaporation obtains was with 1.3 hours
-1Volume space velocity by above-mentioned ion exchange column, carry out ion-exchange, collect the solution after the exchange.The acetate moiety concentration of utilizing HPLC (high-efficient liquid phase analysis instrument) method to record in the solution after the exchange is 10 mg/litre, and the content of lactate ion is 0.2 mg/litre, and the content of succinic ion is 0.2 mg/litre.
(3) preparation fermenation raw liquid and fermentation
Be that solution after 1500 microns crush maize product and the 220g exchange is mixed to get farinaceous size with the 100g average particle diameter.Under 50 ℃, above-mentioned farinaceous size is mixed with the α-amylase (Novozymes Company buys) of 100,000 enzyme activity units, obtain mixture, regulate the pH value to 5 of mixture, and kept 50 minutes, obtain enzymolysis product; Make the temperature of enzymolysis product be down to 33 ℃, with the weighing scale of every gram enzymolysis product, inoculation 10
5The yeast saccharomyces cerevisiae of colony-forming unit (the super highly active dry yeast in Angel, Hubei Angel Yeast stock company), the gained mixture is treated fermentation ends 33 ℃ of lower cultivations 65 hours, the wine degree that adopts oenometer to record tunning is 14.05 volume %.
Embodiment 4
This embodiment is used for illustrating the reuse method of water of condensation provided by the invention.
(1) preparation of the activation of resin and ion exchange resin bed layer
Be that the epoxies that the hydrochloric acid soln of 4 % by weight soaks 800 grams are weakly-basic anion exchange dried resin (Shanghai Resin Factory with the concentration of 2L, the trade mark 331, the quality complete exchange capacity is more than or equal to 9.0 mmoles/every gram dried resin), soaking after 4 hours with deionized water rinsing to pH value is between the 4-6, be after the sodium hydroxide solution 2L of 5 % by weight soaks 6 hours with concentration again, be between the 7-9 with water wash to leacheate pH value, the epoxy after obtaining activating is weak base anion-exchange resin.With the epoxy after the above-mentioned activation be weak base anion-exchange resin 25 gram to load into diameter be 2.18 centimetres, highly be 105 centimetres ion exchange resin bed layer.
(2) ion-exchange
Making temperature is in 50 ℃ the Ethanol Production by Fermentation process, the secondary steam water of condensation that the cleaner liquid evaporation that produces after the useless tank liquor process press filtration in the tower reactor obtains (wherein, Determination of Ac is 470 mg/litre, the content of lactate ion is 375 mg/litre, and the content of succinic ion is 115 mg/litre) with 3 hours
-1Volume space velocity by above-mentioned ion exchange column, carry out ion-exchange, collect the solution after the exchange.The acetate moiety concentration of utilizing HPLC (high-efficient liquid phase analysis instrument) method to record in the solution after the exchange is 15 mg/litre, and the content of lactate ion is 0.8 mg/litre, and the content of succinic ion is 0.8 mg/litre.
(3) preparation fermenation raw liquid and fermentation
Be that solution after 1500 microns crush maize product and the 220g exchange is mixed to get farinaceous size with the 100g average particle diameter.Under 50 ℃, above-mentioned farinaceous size is mixed with the α-amylase (Novozymes Company buys) of 100,000 enzyme activity units, obtain mixture, regulate the pH value to 5 of mixture, and kept 50 minutes, obtain enzymolysis product; Make the temperature of enzymolysis product be down to 33 ℃, with the weighing scale of every gram enzymolysis product, inoculation 10
5The yeast saccharomyces cerevisiae of colony-forming unit (the super highly active dry yeast in Angel, Hubei Angel Yeast stock company), the gained mixture is treated fermentation ends 33 ℃ of lower cultivations 65 hours, the wine degree that adopts oenometer to record tunning is 13.98 volume %.
Embodiment 5
This embodiment is used for illustrating the reuse method of water of condensation provided by the invention.
(1) preparation of the activation of resin and ion exchange resin bed layer
Concentration with 2L is strongly basic anions exchange dried resin (the Jiangsu Su Qing of hydrochloric acid soln immersion 800 grams of 4 % by weight, trade mark D201, the quality complete exchange capacity is more than or equal to 3.8 mmoles/every gram dried resin), soaking after 4 hours with deionized water rinsing to pH value is between the 4-6, be after the sodium hydroxide solution 2L of 5 % by weight soaks 6 hours with concentration again, it is between the 7-9 that water cleans drip washing to leacheate pH value, the strongly basic anion exchange resin after obtaining activating.Loading into diameter with strongly basic anion exchange resin 25 grams after the above-mentioned activation is 2.18 centimetres, highly is 115 centimetres ion exchange resin bed layer.
(2) ion-exchange
Making temperature is in 50 ℃ the Ethanol Production by Fermentation process, the secondary steam water of condensation that the cleaner liquid evaporation that produces after the useless tank liquor process press filtration in the tower reactor obtains (wherein, Determination of Ac is 470 mg/litre, the content of lactate ion is 380 mg/litre, and the content of succinic ion is 117 mg/litre) with 1.7 hours
-1Volume space velocity by above-mentioned ion exchange column, carry out ion-exchange, collect the solution after the exchange.Utilizing the acetate moiety concentration in the solution after the HPLC method records exchange is 18 mg/litre, and the content of lactate ion is 2 mg/litre, and the content of succinic ion is 2 mg/litre.
(3) preparation fermenation raw liquid and fermentation
Be that solution after 1500 microns crush maize product and the 220g exchange is mixed to get farinaceous size with the 100g average particle diameter.Under 50 ℃, above-mentioned farinaceous size is mixed with the α-amylase (Novozymes Company buys) of 100,000 enzyme activity units, obtain mixture, regulate the pH value to 5 of mixture, and kept 50 minutes, obtain enzymolysis product; Make the temperature of enzymolysis product be down to 33 ℃, with the weighing scale of every gram enzymolysis product, inoculation 10
5The yeast saccharomyces cerevisiae of colony-forming unit (the super highly active dry yeast in Angel, Hubei Angel Yeast stock company), the gained mixture is treated fermentation ends 33 ℃ of lower cultivations 65 hours, the wine degree that adopts oenometer to record tunning is 13.82 volume %.
The result of embodiment 1-5 and Comparative Examples 1-2 shows, use the reuse method of water of condensation provided by the invention, can be so that obtain close ferment effect with the fermenation raw liquid of water of condensation preparation after anionite-exchange resin contacts with the fermenation raw liquid that fresh deionized water is prepared, and significantly better than the water of condensation that does not contact with anionite-exchange resin.
Claims (7)
1. the reuse method of a water of condensation, described water of condensation is the water of condensation that obtains after fermented liquid and/or the distillation of cleaner liquid process and the evaporation concentration, it is characterized in that, the method comprises: this water of condensation is contacted with anionite-exchange resin, the condition of contact so that the content of acetate moiety, lactate and succinic ion in the water of condensation after the contact respectively less than or equal to 20 mg/litre, and will be used for the water of condensation after anionite-exchange resin contacts the preparation fermenation raw liquid, wherein, described anionite-exchange resin is the acrylic acid series weak base anion-exchange resin.
2. reuse method according to claim 1, wherein, the water of condensation that described water of condensation obtains for the cleaner liquid evaporation that produces in the Ethanol Production by Fermentation process.
3. reuse method according to claim 1 and 2, wherein, the condition that water of condensation contacts with anionite-exchange resin comprises: the temperature of contact is 20-60 ℃, the weight ratio of water of condensation and anionite-exchange resin dry weight is 1:0.0036-0.0125.
4. reuse method according to claim 3, wherein, the condition that water of condensation contacts with anionite-exchange resin comprises: the temperature 25-40 of contact ℃, the weight ratio of water of condensation and anionite-exchange resin dry weight is 1:0.0045-0.0075.
5. reuse method according to claim 3, wherein, the mode that water of condensation is contacted with anionite-exchange resin is for making water of condensation pass through the anion exchange resin bed layer, and the condition of described contact comprises that also the volume space velocity of water of condensation is 1.3-3 hour
-1
6. reuse method according to claim 5, wherein, the volume space velocity of water of condensation is 1.6-2.3 hour
-1
7. reuse method according to claim 1, wherein, described acrylic acid series weak base anion-exchange resin is macroporous type acrylic acid series weak base anion-exchange resin, and the weak base group exchange capacity of this macroporous type acrylic acid series weak base anion-exchange resin is more than or equal to 6.5 mmoles/gram dried resin.
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| CN106086091A (en) * | 2016-06-17 | 2016-11-09 | 青岛琅琊台集团股份有限公司 | A kind of itaconic acid concentrates the condensed water method for itaconic acid fermentation |
| CN109650489A (en) * | 2018-12-12 | 2019-04-19 | 安徽华塑股份有限公司 | The method for reducing chloride ion in salt making apparatus saliferous condensed water |
| CN113321339B (en) * | 2021-05-06 | 2022-04-29 | 江南大学 | Method for producing fuel ethanol by recycling evaporated condensed water and reusing evaporated condensed water |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1051029A (en) * | 1989-10-17 | 1991-05-01 | 陶氏化学公司 | The condensation water purification method |
| CN1210848A (en) * | 1998-08-20 | 1999-03-17 | 南亚塑胶工业股份有限公司 | Method and device for removing formic acid and acetic acid from water of glycol production |
| CN101585564A (en) * | 2008-05-22 | 2009-11-25 | 株式会社荏原制作所 | Method and apparatus for condensate demineralization |
| CN101798148A (en) * | 2010-03-26 | 2010-08-11 | 广西大学 | Method for producing drinking water by utilizing steam condensation water of sugar refinery |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1051029A (en) * | 1989-10-17 | 1991-05-01 | 陶氏化学公司 | The condensation water purification method |
| CN1210848A (en) * | 1998-08-20 | 1999-03-17 | 南亚塑胶工业股份有限公司 | Method and device for removing formic acid and acetic acid from water of glycol production |
| CN101585564A (en) * | 2008-05-22 | 2009-11-25 | 株式会社荏原制作所 | Method and apparatus for condensate demineralization |
| CN101798148A (en) * | 2010-03-26 | 2010-08-11 | 广西大学 | Method for producing drinking water by utilizing steam condensation water of sugar refinery |
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