CN102260139A - Separation method of alcoholic fermented liquor - Google Patents
Separation method of alcoholic fermented liquor Download PDFInfo
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- CN102260139A CN102260139A CN2010101834801A CN201010183480A CN102260139A CN 102260139 A CN102260139 A CN 102260139A CN 2010101834801 A CN2010101834801 A CN 2010101834801A CN 201010183480 A CN201010183480 A CN 201010183480A CN 102260139 A CN102260139 A CN 102260139A
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- 238000000034 method Methods 0.000 claims abstract description 50
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- FRXSZNDVFUDTIR-UHFFFAOYSA-N 6-methoxy-1,2,3,4-tetrahydroquinoline Chemical compound N1CCCC2=CC(OC)=CC=C21 FRXSZNDVFUDTIR-UHFFFAOYSA-N 0.000 claims abstract 8
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 claims description 56
- 239000000243 solution Substances 0.000 claims description 43
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- 229920002401 polyacrylamide Polymers 0.000 claims description 31
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 22
- 238000001035 drying Methods 0.000 claims description 10
- 229920000768 polyamine Polymers 0.000 claims description 10
- 239000007790 solid phase Substances 0.000 claims description 6
- 238000004821 distillation Methods 0.000 claims description 5
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- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 abstract description 15
- 239000000126 substance Substances 0.000 abstract description 6
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- 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
- Y02P60/00—Technologies relating to agriculture, livestock or agroalimentary industries
- Y02P60/80—Food processing, e.g. use of renewable energies or variable speed drives in handling, conveying or stacking
- Y02P60/87—Re-use of by-products of food processing for fodder production
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- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The invention discloses a separation method of an alcoholic fermented liquor, comprising the steps of mixing the alcoholic fermented liquor with a flocculating agent solution and processing the mixture according to any one of the following ways: way 1) standing the mixture for layering to obtain supernatant liquor and subnatant bacterial body fluid, discharging the supernatant liquor and carrying out condensation, and carrying out solid-liquid separation on the subnatant bacterial body fluid; and way 2) directly carrying out solid-liquid separation on the mixture. The flocculating agent is a substance that can flocculate and or precipitate thalline in the alcoholic fermented liquor. Compared with the present common separation methods, the method overcomes that normal production can not be satisfied due to difficult direct filtering, increasement of ash content and deepending of color in the subsequent forage, reduction of the quality of the forage and extremely high cost when using sodium hydroxide to raise PH value existing in the prior art, and is simple and practical and has low investment of device. Compared with the prior art, the method can reduce cost by about 70%.
Description
Technical field
The present invention relates to a kind of separation method of zymamsis mash.
Background technology
Alcohol is a kind of important basic industry raw material, is widely used in medicine, daily use chemicals, printing ink paint, chemical intermediate or the like field, also can be used as wine base, leaching agent, washing composition, solvent, tensio-active agent or the like.The main source of industrial spirit is that oil obtains through cracking long-chain organic compound under catalyzer and hot conditions, International Crude Oil significantly soars in the recent period, energy problem and national economy are closely bound up, and the development of substitute energy is just receiving increasing concern.Because world petroleum resource reduces year by year, and non-renewable, alcohol fuel becomes one of best substitute energy.
Alcohol is commonly called as alcohol fuel, is that fermenting raw materials prepares with wheat, corn, Chinese sorghum, potato class or vegetable fibre etc., is called as green energy resource.With the use that is mixed by a certain percentage of alcohol fuel and gasoline, can form a kind of novel vehicle fuel---ethanol petrol.Ethanol petrol is again an environment-friendly fuel, just is widely used, so corn alcohol, just have typical substitute energy notion.Studies show that after ethanol was called in gasoline, octane value and oxygen level in the gasoline obviously raise, can promote the burning of gasoline, but also can reduce emission of automobile wastes, that is to say, ethanol not only can play energy-saving effect, but also can play environment protecting.Under the background of the city atmospheric environment of oil price height and vehicle exhaust puzzlement at present, promoting ethanol petrol also just becomes trend of the times.
Fermentation method prepares alcohol fuel, solid-liquid separation after its fermented liquid distillation is the important step in the Alcohol Production process, raise its pH value with method commonly used at present, the increase filtering velocity reduces the energy consumption in the filtration procedure, has increased the ash content in the DDGS feed simultaneously and quickened Maillard reaction to cause DDGS feed color and luster to be deepened.If can seek a kind of effective separation method, neither use adjust pH, can improve the DDGS feeding quality again, the lower market competitiveness that will strengthen greatly of solid-liquid separation energy consumption in the industry.
At present, the alcohol industry tower bottoms, promptly the zymamsis mash is difficult to handle by the mode of direct filtration.Usually before filtration, regulate the pH value of zymamsis mash to 5.0-6.0 with sodium hydroxide earlier, with the viscosity of reduction zymamsis mash, and then filter, still, when adopting conventional equipment to filter, the flow of mash is still slower, that is, and and filtration difficulty, efficient is lower, and cost is higher.In addition, adopt the ash content in the filter cake that this method obtains higher, and influenced the quality of the fodder that is obtained by this filter cake, hydro-oxidation sodium raises with wherein acid-respons heat release feed temperature simultaneously, the rising of pH value all can be quickened Maillard reaction and produce a large amount of pigments, causes DDGS feed color and luster to be deepened.
Summary of the invention
The objective of the invention is to overcome the solid-liquid separation difficulty of separation method of the zymamsis mash of prior art, the defective that separation efficiency is lower, hydro-oxidation sodium and acid-respons heat release feed temperature wherein raise simultaneously, the rising of pH value all can be quickened Maillard reaction and produce a large amount of pigments, cause DDGS feed color and luster to be deepened, can either effectively separate the separation method that the zymamsis mash can improve the zymamsis mash of feeding quality and provide a kind of.
The invention provides a kind of separation method of zymamsis mash, wherein, this method comprises mixes the zymamsis mash with flocculant solution, and the mixture that obtains is handled according to following any one mode:
Mode 1), forms supernatant liquid and lower floor's thalline liquid with the mixture standing demix; Supernatant liquid is discharged and concentrated, lower floor's thalline liquid is carried out solid-liquid separation;
Mode 2) directly mixture is carried out solid-liquid separation;
Described flocculation agent is for making thalline flocculation and/or the settled material in the zymamsis mash.
After raising fermentation liquid pH, the employing sodium hydroxide that method of the present invention has overcome prior art directly carries out difficulty of filtering separation, cost is higher, and the ash content of coal in the filter cake that can be used as feed that obtains is higher, the feed color and luster is deepened, the defective that feeding quality is reduced, the present invention adopts mode 1) by the zymamsis mash is mixed with flocculant solution the thalline in the fermented liquid is flocculated, make the thalline natural subsidence, thereby reaching the thalline that makes in the zymamsis mash effectively separates with clear liquid, directly upward arrange supernatant liquid then, and concentrate, make it to enter post-order process, and lower floor's thalline liquid carried out solid-liquid separation, with the filter cake oven dry that obtains, and can be used as feed; Employing mode 2) by the zymamsis mash is mixed with flocculant solution the thalline in the fermented liquid is flocculated, directly the mixture with mixing carries out solid-liquid separation, thereby reaching the thalline that makes in the zymamsis mash effectively separates with clear liquid, directly clear liquid is concentrated then, make it to enter post-order process, with the filter cake oven dry that obtains, and can be used as feed.Adopt above-mentioned two kinds of methods all can effectively separate the zymamsis mash, and can obtain low ash content, high-quality feed, and greatly reduce production cost.
Description of drawings
Fig. 1 is the schema of the separation method of zymamsis mash provided by the invention.
Embodiment
According to the present invention, the separation method of described zymamsis mash comprises the zymamsis mash is mixed with flocculant solution, and the mixture that obtains is handled according to following any one mode:
Mode 1), forms supernatant liquid and lower floor's thalline liquid with the mixture standing demix; Supernatant liquid is discharged and concentrated, lower floor's thalline liquid is carried out solid-liquid separation;
Mode 2) directly mixture is carried out solid-liquid separation;
Described flocculation agent is for making the thalline flocculation in the zymamsis mash, settled material.
The present inventor finds, flocculation agent is mixed with the zymamsis mash with the form of flocculant solution, can make it more even with zymamsis mash blended, makes the thalline in this fermentation liquid settled more abundant, complete.
According to the present invention, the solvent in the described flocculant solution can be the various solvents that can form solution with flocculation agent, and generally, the solvent in the described flocculant solution is a water.Described flocculation agent can be various can be with the thalline in zymamsis mash flocculation, sedimentation, and make its effective isolating flocculation agent from fermentation liquid, under the preferable case, described flocculation agent can be selected from one or more in polyacrylamide, polymerize aluminum chloride and the polyamine.
More preferably under the situation, described polyacrylamide is an anion-polyacrylamide, and the number-average molecular weight of described anion-polyacrylamide can be 1,000 ten thousand-2,000 ten thousand, is preferably 1,300 ten thousand-1,700 ten thousand.Described polymerize aluminum chloride is a kind of inorganic flocculating agent, and its molecular formula is [Al
2(OH)
nCl
6-n]
m, wherein, n is 1-5, m≤10, basicity B=n/6 * 100%.The number-average molecular weight of described polyamine can be 3,000,000-6,000,000.
The present inventor finds, polymerize aluminum chloride is easier to make the fine particle thing in the zymamsis mash accumulate in the suspended substance that it forms larger particles on every side, and the easier suspended substance sedimentation that makes larger particles of polyacrylamide, therefore, in the ban after the aqueous solution with zymamsis mash and polymerize aluminum chloride, with the aqueous solution of polyacrylamide, can play better separating effect again.In addition, the present inventor also finds, the weight ratio of polymerize aluminum chloride and polyacrylamide is controlled at greater than 4 to 20 in this flocculant solution, and in the time of more preferably in the scope of 10-20, the layering of thalline and clear liquid is more clear, and promptly separating effect is better.
Under the preferable case, after aqueous solution with zymamsis mash and polymerize aluminum chloride, before the aqueous solution of polyacrylamide, the step that also comprises stirring, more thorough with the gathering that fully makes the fine particle thing in polymerize aluminum chloride and the zymamsis mash, destroy in order to be beneficial to the polymerize aluminum chloride fine particle thing that fully flocculates, can not destroy again simultaneously the particulate matter of having flocculated, the time of described stirring is preferably 0.5-5 minute.
In the present invention, the solubleness of flocculation agent in water is bigger, therefore, the adjustable extent broad of the quality volumetric concentration of described flocculant solution, as, can be for 0.1-5% (m/v), for taking all factors into consideration of cost and effect, the quality volumetric concentration of described polyacrylamide flocculant solution and polyamine flocculant solution is preferably 0.1-0.5% (m/v), and the quality volumetric concentration of described flocculant of polymeric aluminium chloride solution is preferably 1-5% (m/v).
According to method of the present invention, the adjustable extent broad of the consumption of described flocculant solution, for example, can be according to the consumption of how much regulating flocculant solution of the amount of thalline in the zymamsis mash, under the preferable case, with every cubic metre of zymamsis mash is benchmark, the consumption of described flocculant solution makes that the amount of flocculation agent is 20-1000ppm, more preferably under the situation, the consumption of described flocculant solution makes that the amount of polyacrylamide flocculant and polyamine flocculation agent is 20-100ppm, makes that the amount of flocculant of polymeric aluminium chloride is 200-1000ppm.
The quality volumetric concentration of thalline is generally 3-10% (m/v) in the described zymamsis mash.
Above-mentioned m/v refers to the quality volumetric concentration, and concrete implication comprises the quality of thalline in the quality of flocculation agent in every liter of flocculant solution or the every liter of zymamsis mash.
According to the present invention, zymamsis mash and flocculant solution blended condition can be comprised blended time and blended temperature, for example, the described blended time can be 1-30 minute, more preferably 1-10 minute; Described blended temperature can be 30-90 ℃, more preferably 60-90 ℃.In order to make zymamsis mash and flocculant solution blended more even, described zymamsis mash and mixing preferably of flocculant solution are under agitation carried out.
According to the present invention, zymamsis mash and flocculant solution blended mode are not particularly limited, for example, can be static mixing, also can be dynamic mixing, also or the combination of two kinds of hybrid modes.Wherein, described static mixing can for: zymamsis mash and flocculant solution at container, as are left standstill and mix in the equipment and leave standstill; Described dynamic mixing can for: will in another transport pipe, converge with being incorporated in the flow process from the zymamsis mash of different transport pipes and flocculant solution and mix, perhaps zymamsis mash and flocculant solution mix by line mixer, and this mixture is delivered in the equipment of leaving standstill leaves standstill.
According to the present invention, in mode 1) in, as long as the zymamsis mash is mixed the mixture standing demix that obtains with flocculant solution condition can guarantee and will form supernatant liquid and lower floor's thalline liquid with the mixed zymamsis mash of flocculant solution.The described time that the mixture that obtains is left standstill can be 1-60 minute, more preferably 20-50 minute.
According to the present invention, in mode 1) in, the method that lower floor's thalline liquid is carried out solid-liquid separation can adopt the whole bag of tricks of this area routine, for example, filter or centrifugation method, the method for described solid-liquid separation and condition are following as long as the turbidity of the filtrate that obtains after feasible the filtration is 800NTU.For example, can adopt plate-and-frame filter press to filter in the specific embodiment of the present invention, filtering condition comprises sheet frame veneer model 80cm * 120cm, sheet frame maximum working pressure (MWP) 0.4Mpa, veneer filter cloth filtration area is generally 0.96 square metre, 758 model filter clothes.
In addition, in mode 1) in, because the relative supernatant liquid of viscosity of lower floor's thalline liquid wants big, adopting the centrifugal mode to carry out solid-liquid separation can be more convenient, for example, thalline liquid can be carried out solid-liquid separation by horizontal screw centrifuge.Its concrete operation method and condition are conventionally known to one of skill in the art, here repeat no more.
In mode 2) in, the method that the mixture that obtains is directly carried out solid-liquid separation can adopt the whole bag of tricks of this area routine, for example, filter or centrifugation method, the method for described solid-liquid separation and condition are following as long as the turbidity of the filtrate that obtains after feasible the filtration is 800NTU.For example, can adopt plate-and-frame filter press to filter in the specific embodiment of the present invention, filtering condition comprises sheet frame veneer model 80cm * 120cm, sheet frame maximum working pressure (MWP) 0.4Mpa, veneer filter cloth filtration area is generally 0.96 square metre, 758 model filter clothes.
According to the present invention, in mode 1) in, this method also comprise lower floor's thalline liquid carried out solid-liquid separation after, the solid phase that obtains is carried out drying, and the liquid phase that obtains is carried out spissated step; In mode 2) in, this method also comprise mixture carried out solid-liquid separation after, the solid phase that obtains is carried out drying, the liquid phase that obtains is concentrated.Described exsiccant method and condition all can adopt method well known in the art and condition to carry out.For example, the exsiccant mode can be seasoning, forced air drying, the drying mode of various routines such as vacuum-drying.Described exsiccant condition can comprise that the exsiccant temperature is 80-100 ℃, and the exsiccant time can be 1-5 hour.
In the present invention, the method that supernatant liquid is discharged comprises by suction unit extracts supernatant liquid out, perhaps by opening discharge line supernatant liquid is discharged.
Spissated method is generally the quadruple effect evaporation concentration, one imitate temperature can 85-95 ℃, two imitate temperature can 75-85 ℃, the triple effect temperature can 65-75 ℃, the quadruple effect temperature can 55-65 ℃, being concentrated into dry is 30-45 weight %.
In the present invention, after described zymamsis mash referred in distillation tower alcohol steamed, the solidliquid mixture in the tower still, described thalline obtained solid-phase mixture after referring in distillation tower alcohol steamed in the tower still.
To further describe in detail the present invention by specific embodiment below, following examples only are used to illustrate the present invention, but are not used for limiting the scope of the invention.
The veneer filtration area of used plate-and-frame filter press is 0.96 square metre among following embodiment and the Comparative Examples 1-2, sheet frame veneer model 80cm * 120cm, sheet frame maximum working pressure (MWP) 0.4Mpa, 758 model filter clothes.
The measuring method of cell concentration is GB/T741-2003 in the zymamsis mash.
The turbidity testing method detects for adopting turbidimeter (WGZ-200 turbidimeter).
Adopt GB/T 9825-1988 to measure with the ash oontent in the feed that obtains behind the filtration cakes torrefaction (butt with feed is a benchmark).
Adopt GB/T 5009.5-1985 to measure with the protein content in the feed that obtains behind the filtration cakes torrefaction (butt with feed is a benchmark).
Supereloc, flocculant of polymeric aluminium chloride and polyamine flocculation agent used among the following embodiment are respectively available from Anhui Tian Run chemical inc, Ciba (China) company limited and Kemira company.
Embodiment 1
Present embodiment is used to illustrate the separation method of zymamsis mash provided by the invention.
(1) 500ml zymamsis mash [cell concentration is 5.32% (m/v)] is placed retort.
(2) be that 1,500 ten thousand anionic polyacrylamide flocculation agent is soluble in water with molecular weight, make mass volume ratio concentration and be 0.2% solution; And under 70 ℃, in the zymamsis mash, add described flocculant aqueous solution, and be benchmark with every cubic metre of fermented liquid, the consumption of described flocculant aqueous solution (12.5ml) makes that the amount of flocculation agent is 50ppm, mixes 10 minutes.
(3) mixed solution that step (2) is obtained is inserted in the flame filter press and is filtered, and the clear liquid filtering velocity is 15s/100ml, and till fermentation liquid had advanced, the turbidity of the clear liquid that obtains was 534NTU.
(4) filter cake that step (3) is obtained is dried down at 95 ℃ and is obtained feed (10 weight % moisture), and the ash oontent that gets in the feed with the butt instrumentation is that 2.85% (m/m), protein content are 28.91% (m/m).
Embodiment 2
Present embodiment is used to illustrate the separation method of zymamsis mash provided by the invention.
(1) 500ml zymamsis mash [cell concentration is 5.32% (m/v)] is placed retort.
(2) be that 1,500 ten thousand anionic polyacrylamide flocculation agent is soluble in water with molecular weight, make mass volume ratio concentration and be 0.2% solution; And under 70 ℃, in the zymamsis mash, add described flocculant aqueous solution, and be benchmark with every cubic metre of fermented liquid, the consumption of described flocculant aqueous solution (25ml) makes that the amount of flocculation agent is 100ppm, mixes 10 minutes.
(3) mixed solution that step (2) is obtained is inserted in the flame filter press and is filtered, and the clear liquid filtering velocity is 12s/100ml, and till fermentation liquid had advanced, the turbidity of the clear liquid that obtains was 520NTU.
(4) filter cake that step (3) is obtained is dried down at 95 ℃ and is obtained feed (10 weight % moisture), and the ash oontent that gets in the feed with the butt instrumentation is that 2.84% (m/m), protein content are 29.06% (m/m).
Embodiment 3
Present embodiment is used to illustrate the separation method of zymamsis mash provided by the invention.
Method according to embodiment 1 is separated the zymamsis mash, and different is, is benchmark with every cubic metre of fermented liquid, and the consumption of described flocculant aqueous solution (5ml) makes that the amount of flocculation agent is 20ppm.The clear liquid filtering velocity is 29s/100ml, and the turbidity of the clear liquid that obtains is 660NTU.Is 2.87% (m/m), protein content 27.29% (m/m) with filter cake at the ash oontent that 90 ℃ of following dryings obtain in the feed.
Embodiment 4
Present embodiment is used to illustrate the separation method of zymamsis mash provided by the invention.
Method according to embodiment 2 is separated the zymamsis mash, different is, used flocculant aqueous solution is that (n is 1-5 to polymerize aluminum chloride, m≤10, basicity B=n/6 * 100%) the aqueous solution, making mass volume ratio concentration and be 2% polymeric aluminum chlorides solution, is benchmark with every cubic metre of fermented liquid, and the consumption of described flocculant aqueous solution (12.5ml) makes that the amount of flocculation agent is 500ppm.The clear liquid filtering velocity is 39s/100ml, and the turbidity of the clear liquid that obtains is 746NTU.Is that 2.93% (m/m), protein content are 27.25% (m/m) with filter cake at the ash oontent that 90 ℃ of following dryings obtain in the feed.
Embodiment 5
Present embodiment is used to illustrate the separation method of zymamsis mash provided by the invention.
Method according to embodiment 2 is separated the zymamsis mash, different is to be to add the aqueous solution of polymerize aluminum chloride earlier with flocculant aqueous solution and fermentation liquid blended mode, and to mix 1-2 minute, and then the aqueous solution of adding polyacrylamide, mixed 10 minutes; With every cubic metre of fermented liquid is benchmark, and the consumption of the aqueous solution of described polymerize aluminum chloride (12.5 milliliters) makes that the amount of flocculation agent is 500ppm, and the consumption of the aqueous solution of described polyacrylamide (12.5 milliliters) makes that the amount of flocculation agent is 50ppm.The clear liquid filtering velocity is 15s/100ml, and the turbidity of the clear liquid that obtains is 480NTU.Is that 2.71% (m/m), protein content are 29.52% (m/m) with filter cake at the ash oontent that 90 ℃ of following dryings obtain in the feed.
Embodiment 6
Present embodiment is used to illustrate the separation method of zymamsis mash provided by the invention.
Method according to embodiment 5 is separated the zymamsis mash, different is to be to add the aqueous solution of polymerize aluminum chloride earlier with flocculant aqueous solution and fermentation liquid blended mode, and to mix 1-2 minute, and then the aqueous solution of adding polyacrylamide, mixed 10 minutes; With every cubic metre of fermented liquid is benchmark, and the consumption of the aqueous solution of described polymerize aluminum chloride (25 milliliters) makes that the amount of flocculation agent is 1000ppm, and the consumption of the aqueous solution of described polyacrylamide (12.5 milliliters) makes that the amount of flocculation agent is 50ppm.The clear liquid filtering velocity is 10s/100ml, and the turbidity of the clear liquid that obtains is 400NTU.Is that 2.75% (m/m), protein content are 28.85% (m/m) with filter cake at the ash oontent that 90 ℃ of following dryings obtain in the feed.
Embodiment 7
Present embodiment is used to illustrate the separation method of zymamsis mash provided by the invention.
Method according to embodiment 5 is separated the zymamsis mash, different is to be to add the aqueous solution of polymerize aluminum chloride earlier with flocculant aqueous solution and fermentation liquid blended mode, and to mix 1-2 minute, and then the aqueous solution of adding polyacrylamide, mixed 10 minutes; With every cubic metre of fermented liquid is benchmark, and the consumption of the aqueous solution of described polymerize aluminum chloride (5 milliliters) makes that the amount of flocculation agent is 200ppm, and the consumption of the aqueous solution of described polyacrylamide (12.5 milliliters) makes that the amount of flocculation agent is 50ppm.The clear liquid filtering velocity is 16s/100ml, and the turbidity of the clear liquid that obtains is 490NTU.Is that 2.8% (m/m), protein content are 28.10% (m/m) with filter cake at the ash oontent that 90 ℃ of following dryings obtain in the feed.
Embodiment 8
Present embodiment is used to illustrate the separation method of zymamsis mash provided by the invention.
(1) will produce greatly in zymamsis mash [cell concentration is 4.5-5.5% (m/v)] and flocculant aqueous solution (with molecular weight is that 1,500 ten thousand anionic polyacrylamide flocculation agent is soluble in water, make mass volume ratio concentration and be 0.2% solution) by mixing in the line mixer, with every cubic metre of fermented liquid is benchmark, make that the consumption of flocculation agent is 50ppm, the mixture that obtains squeezed in the plate-and-frame filter press by volume pump filter, the fermentation liquid treatment capacity is 260-280m
3/ h, the average turbidity of the clear liquid that obtains is 570NTU.
(2) filter cake is dried under 95 ℃ of temperature and was obtained feed (10 weight % moisture) in 2-4 hour, and the ash oontent that records in the feed is that 3-4% (m/m), albumen average content are 27-28% (m/m), color and luster tawny.
Embodiment 9
Present embodiment is used to illustrate the separation method of zymamsis mash provided by the invention.
(1) 500ml zymamsis mash [cell concentration is 5.32% (m/v)] is placed retort.
(2) be that 5,000,000 polyamine flocculation agent is soluble in water with number-average molecular weight, make mass volume ratio concentration and be 0.2% solution; And under 70 ℃, in the zymamsis mash, add described flocculant aqueous solution, and be benchmark with every cubic metre of fermented liquid, the consumption of described flocculant aqueous solution (12.5ml) makes that the amount of flocculation agent is 50ppm, mixes after 10 minutes and leaves standstill 25 minutes.
(3) mixed solution after the leaving standstill of step (2) is layered as supernatant liquid and lower floor's thalline liquid, supernatant liquid is discharged, lower floor's thalline liquid entered carry out solid-liquid separation (centrifuge speed 1800-2400rpm) in the horizontal screw centrifuge, the turbidity of the clear liquid that obtains is 630NTU.
(4) filter cake that step (3) is obtained is dried down at 95 ℃ and is obtained feed (10 weight % moisture), and the ash oontent that gets in the feed with the butt instrumentation is that 2.84% (m/m), protein content are 27.94% (m/m).
Embodiment 10
Present embodiment is used to illustrate the separation method of zymamsis mash provided by the invention.
(1) 500ml zymamsis mash [concentration of thalline is 5.32% (m/v)] is placed retort.
(2) under 70 ℃, the aqueous solution with polymerize aluminum chloride joins in the described fermentation liquid earlier, and mixes 1-2 minute, and then adds the aqueous solution of polyacrylamide, mixes after 10 minutes and leaves standstill 50 minutes.With every cubic metre of fermented liquid is benchmark, (n is 1-5 to described polymerize aluminum chloride, m≤10, the consumption (12.5 milliliters) of aqueous solution basicity B=n/6 * 100%) (mass volume ratio concentration is 2% polymeric aluminum chlorides solution) makes that the amount of flocculation agent is 500ppm, the consumption (12.5 milliliters) of the aqueous solution of described polyacrylamide (with number-average molecular weight is that 1,500 ten thousand anionic polyacrylamide flocculation agent is soluble in water, makes mass volume ratio concentration and be 0.2% solution) makes that the amount of flocculation agent is 50ppm.
(3) mixed solution after the leaving standstill of step (2) is layered as supernatant liquid and lower floor's thalline liquid, and supernatant liquid is discharged, and the turbidity of the clear liquid that obtains is 720NTU, lower floor's thalline liquid is entered in the plate-and-frame filter press filter, and the turbidity of the clear liquid that obtains is 632NTU.
(4) filter cake that step (3) is obtained is dried down at 95 ℃ and is obtained feed (10 weight % moisture), and the ash oontent that gets in the feed with the butt instrumentation is that 2.89% (m/m), protein content are 28.02% (m/m).
Comparative Examples 1
This Comparative Examples is used to illustrate the separation method of the zymamsis mash of prior art.
(1) 500ml zymamsis mash [cell concentration is 5.32% (m/v)] is placed the retort mixing.
(2) under 70 ℃, will transfer to 5.3 on the fermentation liquid pH in the step (1) with sodium hydroxide.
(3) mixed solution that step (2) is obtained is inserted in the plate-and-frame filter press and is filtered, and the clear liquid filtering velocity is 50s/100ml, and till fermentation liquid had advanced, the turbidity of the clear liquid that obtains was 760NTU.
(4) filter cake that step (3) is obtained is dried down at 95 ℃ and is obtained feed (10 weight % moisture), and the ash oontent that gets in the feed with the butt instrumentation is that 3.24% (m/m), protein content are 27.18% (m/m)
Comparative Examples 2
This Comparative Examples is used to illustrate the separation method of the zymamsis mash of prior art.
(1) will produce greatly in zymamsis mash [concentration of thalline is 4.5-5.5% (m/v)] use calcium hydroxide and sodium hydroxide adjust pH to 5.3 respectively, the mixture that obtains directly squeezed in the plate-and-frame filter press with impeller pump filter, the fermentation liquid treatment capacity is 220-240m
3/ h, the clear liquid average turbidity that obtains is 820NTU.
(2) filter cake is dried under 95 ℃ of temperature and was obtained feed (10 weight % moisture) in 2-4 hour, and the ash oontent that records in the feed is that 5-7% (m/m), protein content are 26-27% (m/m), the color and luster brown.
The result shows: can improve filtration velocity after regulating the pH value, but the raising degree is not as adding flocculation agent.Transfer pH with calcium hydroxide in addition, the higher (SO of calcium contents in the clear liquid
4 2-: 790ppm Ca:2200ppm), can cause easily forming in the follow-up thickener calcium sulfate and stop up or fouling.
Contrast two kinds of technologies as can be seen, adopt method of the present invention can effectively separate the zymamsis mash, simultaneously can improve filtration velocity, and lower, the lighter color of ash oontent in the feed that obtains, quality are better.In addition, method of the present invention can reduce production costs greatly.Adopt flocculence to compare and to reduce production costs about 70% with existing technology.
Claims (13)
1. the separation method of a zymamsis mash is characterized in that, this method comprises mixes the zymamsis mash with flocculant solution, and the mixture that obtains is handled according to following any one mode:
Mode 1), forms supernatant liquid and lower floor's thalline liquid with the mixture standing demix; Supernatant liquid is discharged and concentrated, lower floor's thalline liquid is carried out solid-liquid separation;
Mode 2) directly mixture is carried out solid-liquid separation;
Described flocculation agent is for making thalline flocculation and/or the settled material in the zymamsis mash.
2. method according to claim 1, wherein, described flocculant solution is the aqueous solution of flocculation agent, described flocculation agent is selected from one or more in polyacrylamide type, polymerize aluminum chloride and the polyamine.
3. method according to claim 2, wherein, described polyacrylamide is an anion-polyacrylamide, the number-average molecular weight of described anion-polyacrylamide is 1,000 ten thousand-2,000 ten thousand; The molecular formula of described polymerize aluminum chloride is [Al
2(OH)
nCl
6-n]
m, wherein, n is 1-5, m≤10, basicity B=n/6 * 100%; The number-average molecular weight of described polyamine is 3,000,000-6,000,000.
4. method according to claim 2 wherein, comprises earlier aqueous solution with zymamsis mash and polymerize aluminum chloride with zymamsis mash and flocculant solution blended method, again with the aqueous solution of polyacrylamide; The mass ratio of polymerize aluminum chloride and polyacrylamide is greater than 4 to 20.
5. method according to claim 4 wherein, after the aqueous solution with zymamsis mash and polymerize aluminum chloride, before the aqueous solution of polyacrylamide, also comprises the step of stirring, and the time of described stirring is 1-5 minute.
6. method according to claim 2, wherein, with every cubic metre of zymamsis mash is benchmark, and the consumption of described flocculant solution makes that the amount of polyacrylamide flocculant and polyamine flocculation agent is 20-100ppm, makes that the amount of flocculant of polymeric aluminium chloride is 200-1000ppm; The quality volumetric concentration of polyacrylamide flocculant solution and polyamine flocculant solution is 0.1-0.5%, and the quality volumetric concentration of flocculant of polymeric aluminium chloride solution is 1-5%; The quality volumetric concentration of thalline is 2-10% in the zymamsis mash.
7. method according to claim 1, wherein, described zymamsis mash is static mixing with the hybrid mode of flocculant solution and/or dynamically mixes.
8. according to claim 1 or 7 described methods, wherein, described zymamsis mash carried out with mixing under agitation of flocculant solution, and the blended temperature is 50-90 ℃, and the blended time is 5-30 minute.
9. method according to claim 1, wherein, in mode 1) in, the time of leaving standstill is 20-50 minute.
10. method according to claim 1 is wherein, in mode 1) in, lower floor's thalline liquid is carried out the method for solid-liquid separation and condition make that the turbidity of the filtrate that obtains after filtering is below the 800NTU; In mode 2) in, the mixture that obtains is carried out the method for solid-liquid separation and condition make that the turbidity of the filtrate that obtains after filtering is below the 800NTU.
11. according to claim 1 or 10 described methods, wherein, in mode 1) in, this method also comprise lower floor's thalline liquid carried out solid-liquid separation after, the solid phase that obtains is carried out drying, the liquid phase that obtains is concentrated; In mode 2) in, this method is carried out drying with the solid phase that obtains after comprising that also the mixture that will obtain carries out solid-liquid separation, and the liquid phase that obtains is concentrated.
12. method according to claim 11, wherein, described exsiccant condition comprises that the exsiccant temperature is 90-100 ℃, and the exsiccant time is 2-5 hour.
13. according to any described method in claim 1-5 or 7, wherein, after described zymamsis mash refers in distillation tower alcohol steamed, the solidliquid mixture that obtains at the tower still, after described thalline refers in distillation tower alcohol steamed, the solid-phase mixture that obtains at the tower still.
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| CN105779528A (en) * | 2014-12-22 | 2016-07-20 | 中国石油化工股份有限公司 | Lignocellulose continuous enzymatic hydrolysis and synchronous saccharification-fermentation method |
| CN106244633A (en) * | 2016-08-23 | 2016-12-21 | 广东省生物工程研究所（广州甘蔗糖业研究所） | A kind of reversible regulation and control methods and applications of Yeast Flocculation |
| CN106957129A (en) * | 2017-03-30 | 2017-07-18 | 湖北广济药业股份有限公司 | A kind of processing method of Lactochrome fermentation liquor |
| CN108077588A (en) * | 2017-11-30 | 2018-05-29 | 广西中粮生物质能源有限公司 | A kind of rice alcohol residue separation method |
| CN108094710A (en) * | 2017-12-11 | 2018-06-01 | 广西中粮生物质能源有限公司 | A kind of method of the full vinasse production of LIPIDS OF DRY RICE EMBRYO |
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| CN105779528B (en) * | 2014-12-22 | 2024-05-10 | 中国石油化工股份有限公司 | Continuous enzymolysis and synchronous saccharification and fermentation method for lignocellulose |
| CN106244633A (en) * | 2016-08-23 | 2016-12-21 | 广东省生物工程研究所（广州甘蔗糖业研究所） | A kind of reversible regulation and control methods and applications of Yeast Flocculation |
| CN106244633B (en) * | 2016-08-23 | 2019-06-18 | 广东省生物工程研究所（广州甘蔗糖业研究所） | A kind of reversible regulation methods and applications of Yeast Flocculation |
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| CN108077588A (en) * | 2017-11-30 | 2018-05-29 | 广西中粮生物质能源有限公司 | A kind of rice alcohol residue separation method |
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| CN111454853A (en) * | 2020-04-29 | 2020-07-28 | 杭州经世科技有限公司 | Fermentation and purification process of yeast engineering strain |
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