CN1052859C - Method for producing protein feed by using alcoholic grains liquor and equipment thereof - Google Patents
Method for producing protein feed by using alcoholic grains liquor and equipment thereof Download PDFInfo
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- CN1052859C CN1052859C CN97110190A CN97110190A CN1052859C CN 1052859 C CN1052859 C CN 1052859C CN 97110190 A CN97110190 A CN 97110190A CN 97110190 A CN97110190 A CN 97110190A CN 1052859 C CN1052859 C CN 1052859C
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- liquid separator
- vapour liquid
- pump
- evaporimeter
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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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Abstract
The present invention discloses a method for producing protein feed via evaporating clear liquid obtained by the solid-liquid separation alcoholic grain liquor produced in the production process of alcohol. Aiming at the problems generally existing in alcohol industries at home and abroad, the present invention designs an advanced low-temperature and vacuum evaporating device. The method of the present invention has the characteristics of large circulation volume, low evaporation temperature, etc. so as to ensure the full recovery of soluble protein in the clear liquid, enhance the protein content of dry-powder feed and ensure the color of the feed, and simultaneously solves the problem of scale formation existing in the evaporating device.
Description
The present invention relates to a kind of method of producing protein feed, relate in particular to a kind of method of producing protein feed with alcoholic grains liquor; The present invention also relates to implement the equipment of the inventive method.
Produce a large amount of draff liquids in the Alcohol Production process, the clear liquid after Separation of Solid and Liquid still contains a lot of solid contents, and it is mainly the very high feed of protein content, if not treated and directly discharge, contaminated environment not only, and cause a large amount of wastes.
At present, domestic alcohol industry is produced protein feed to the alcoholic grains liquor evaporation and concentration does not still have successful precedent.Promptly on production method and production equipment, also all there are many insurmountable problems.The package import foreign technology makes again on the price that domestic enterprise is difficult to accept.Given this plant situation, at present, domestic production producer obtains the part solid content after generally adopting natural subsidence or machinery to separate, and clear liquid is directly discharged.The rate of recovery of this processing method only accounts for 3% of alcohol distiller's solution total amount, and not only a large amount of callable solid contents and soluble protein are bled off in vain, causes very big waste, has seriously polluted environment simultaneously, has restricted the development of alcohol industry.In the world, though all having reclaimed alcoholic grains liquor, some developed countries are used to produce dry powder feeding, but from a complete set of operation result of introducing projects of domestic several families, it is loaded down with trivial details that ubiquity device structure complicated technology route, be not suitable for the domestic production situation, do not reach design level, energy consumption is high and operation is unstable, shortcomings such as cost height.Also be difficult to accept in the enterprise at home at present.
The purpose of this invention is to provide a kind of new method of producing protein feed with alcoholic grains liquor, it can produce protein feed energy-efficiently.
Another purpose of the present invention provides a kind of equipment of implementing this method.
In this method of enforcement, our custom-designed equipment has evaporimeter, vapour liquid separator, Mo Shi tower, vacuum jet pump, these corollary equipments are that this method is implemented requisite Special Equipment, its performance, function all reach design level, these four kinds of its principles of special equipment are applied to the production chemical product in chemical industry, and these four kinds of different size equipment of specialized designs are used to produce feed in the present invention.Described herein feed liquid % is meant solid weight in the feed liquid/feed liquid gross weight %.
In the method, its efficient circulation pump, automatically controlled and instrument and meter for automation etc. all adopt domestic equipment, so, this process is except that investment is less, and, in running stably, fully demonstrate high concentration product, low production cost that the advanced technologies technology is brought, compact device structure and for ease of maintenaince wait characteristics.
Technical scheme of the present invention is achieved in that
Isolate clear liquid by seperator or settling tank and enter the clear liquid storage tank, squeeze into I with pump
1Imitate pump inlet, by circulating pump at I
1Single-effect evaporator and I
1Imitate circulation in the vapour liquid separator, I
1The effect vapour liquid separator evaporates indirect steam and enter vacuum system behind the Mo Shi tower, and the feed liquid that part is concentrated enters I quantitative automaticly
2Imitate, material is at I
2Pass through I in the effect
2Imitate circulating pump at I
2Single-effect evaporator, I
2Imitate in the vapour liquid separator and circulate.Separator produces indirect steam and is used to heat I
1Imitate I
2Imitate thermal source and come from the waste gas that is produced in the drying machine course of work.I
2Imitate interior material dosing, automatically send into dry workshop section by automatic instrument(s) by pump.If when material concentration is low, this material can be squeezed into II
1Imitate, at II
1Material repeats I in imitating
1The technical process of imitating, II
1The effect thermal source is II
2Imitate vapour liquid separator and produce indirect steam.II
1Material dosing in imitating, automatically enter II
2Imitate II
2Imitate and repeat I again
2The technical process of imitating, institute's difference is II
2Imitating thermal source is condensed water and small amount of supplemental steam in the drying machine course of work, II
2Imitate material and continuously, quantitatively, automatically join drying system production protein feed by automatic instrument(s).
The concrete production process route of technical solution of the present invention is by providing in detail below in conjunction with accompanying drawing, and wherein, accompanying drawing 1 has been narrated two effect level Four production processes, accompanying drawing 2 has been narrated two independently evaporation processes.Two Figure of description have specifically described the process route that alcoholic grains liquor is formed by several production equipments in detail, thereby concentrate the overall process of making pasty product.
Press accompanying drawing 2 narrations below, use evaporimeter feeding pump 2 with 30～50M the clear liquid that clear liquid groove 1 interior solid content is 0.7%-5.4% solid weight/fluid gross weight (soluble protein is a 1.5%-2.0% weight in the solid content)
3/ h automatic charging is to I
1Imitate circulating pump 4 imports, enter I by this stock liquid
1Imitate the tube side heat exchange, I
1Single-effect evaporator is horizontal, and its tube side is the 3-8 backhaul, at I
1Single-effect evaporator 3 is interior by I
2Imitate vapour liquid separator 9 (1.6 meters-4.8 meters of format diameter, 4 meters-9.2 meters of height) produce indirect steam and be heated to 38-85 ℃ after through I
1Imitate connecting line L
1, I
1Imitate vapour liquid separator 5 with 400-1000M
3/ h circulates.Vapour liquid separator 5 (1.8 meters-5.2 meters of format diameter, 4.6 meters-10.5 meters of height) thermal material is under the pressure of 0.03～0.005MPa (absolute pressure, together later), with 5.5～7.0 tons/hour speed evaporation, the indirect steam that is produced, after entering membrane type tower 19, with 35 ℃, 400-800M
3/ h recirculated water carries out counter current contacting, and recirculated water continues to use after cooling off.Fixed gas is extracted discharging out by one-level jet pump 20, two-stage injection pump 21 or water ring pump 22.I
1The material of imitating preliminary enrichment in the vapour liquid separator 5 is by I
2Imitate feeding pump 6 and add I quantitative automaticly
2Imitate circulating pump 8 imports, enter I by this stock liquid
2The heat exchange of single-effect evaporator tube side, I
2Single-effect evaporator is horizontal, and its tube side is the 3-8 backhaul, at I
2Single-effect evaporator 9 and I
2Imitate connecting line L
2, I
2Imitate in the vapour liquid separator 9 with 400-1000M
3/ h circulation.Feed liquid is at process I
2Behind the single-effect evaporator 7, remove I after being heated to form 70-126 ℃
2Imitate vapour liquid separator 9.Under the pressure of 0.03-0.05MPa, with the 5.2-6.5 ton/hour speed evaporation enrichment, the pasty state fluid to 40% is finished product, controls continuous extraction to drying machine through automatic instrument, the indirect steam that produces as I
1The thermal source of single-effect evaporator 3 and continue to use I
2The thermal source of single-effect evaporator 7 all adopts the 9-11 ton/hour indirect steam of the drying machine course of work.This moment II
1II
2And I
1I
2Imitate and promptly can be used as two and independently two imitate vapo(u)rization systems work simultaneously (shown in Figure of description 2).II
1, II
2Single-effect evaporator is horizontal, and its tube side is the 3-8 backhaul, and shell side is the 2-6 backhaul.
Press accompanying drawing 1 narration now again, as continuous adding I
1Clear liquid concentration is lower than at 4% o'clock, I in the single-effect evaporator 3
2Imitate in the vapour liquid separator 9 material concentrations and be difficult to reach 40% and take out continuously, at this moment, can be with I
2Imitate vapour liquid separator 9 interior materials as II
1Imitate raw material, add II quantitative automaticly
1Imitate circulating pump 12 imports, by circulating pump 12 and II
1Imitate connecting pipeline L
3, II
1Imitate in the vapour liquid separator 13 with 400-1000M
3/ h circulates, II
1Imitating the vapour liquid separator diameter is 1.6 meters-4.2 meters, 4 meters-9.2 meters of height.At II
1Enter II after material is heated to 65-88 ℃ in the single-effect evaporator
1Vapour liquid separator 13, under the pressure of 0.03-0.01Mpa, in the feed liquid moisture content with the 5.3-6.2 ton/hour speed evaporation, the indirect steam that produces directly enters membrane type tower 19, Mo Shi tower specification is 0.8 meter-1.95 meters of diameters, 2.8 meters-5.9 meters of height, 5-10 layer column plate.Steam and recirculated water heat exchange and be condensed in membrane type tower 19, fixed gas is taken away emptying by one-level jet pump 20, two-stage injection pump 21 or water ring pump 22.The feed liquid that is concentrated is continuously passed through II quantitative automaticly
2 Imitate feeding pump 14, add II
2 Imitate circulating pump 16 imports, pass through II
2 Imitate circulating pump 16 connecting line L
4, II
2Imitate in the vapour liquid separator 17 and circulate II
2Imitate 1.4 meters-2.6 meters of vapour liquid separator diameters, height 3.8-5.8 rice, II
2In the evaporimeter 15 materials by 8-10 ton/hour drying machine condensed water and 2-4 ton/hour vapor mixing after after indirect 70-126 ℃, enter II
2Imitate vapour liquid separator 17, under the effect of 0.03-0.04Mpa pressure, feed liquid moisture content is with 5.5-6.8 ton/speed at one hour rating evaporation, the indirect steam that produces as II
1Single-effect evaporator 11 thermals source continue to use, and II
2Imitate the material that is concentrated in the vapour liquid separator 17 and then pass through automatic instrument(s) continuously and automatically with 2-11M
3/ h flow joins and removes to produce dry powder feeding in the drying machine.
The present invention has following feature and beneficial effect:
1, be applicable to the clear liquid of variable concentrations in whole technological design, and adopt 2 effects, 3 to imitate or 4 grades of formula evaporated forms of 2 effects, flexible operation and elasticity are big.
2, Du Te negative pressure system, owing to adopt the membrane type tower, jet pump forms the two-stage negative pressure, has reduced running device quantity widely.
3, choose the big (200-1000m of internal circulating load scope
3).
4, utilize waste heat, I in large quantities
1Imitate II
2Effect is except that per hour replenishing the 2-3 ton steam, and the condensed water and the indirect steam that produce when all the other heats are all worked from drying machine utilize waste heat.
5, adopt different negative pressure grades, at I
1II
1And I
2II
2Form two suction gradients, thereby form different evaporating temperatures.
6, because evaporating temperature is low, not only solve the fouling of evaporator problem, kept the outward appearance of interior protein content of material and product simultaneously to greatest extent.
7, each single-effect evaporator adopts the many backhauls of horizontal installation shell and tube, and good effect of heat exchange realizes energy-saving and cost-reducing.
8, this engineering adopts closed cycle water system, realizes energy-saving and cost-reducing.
Following embodiment is used to describe in detail the present invention, in any case but can not to be understood as be limitation of the present invention.
Embodiment 1 (2 imitate 4 grades of production methods, Fig. 1):
Solid content is that 2.3% clear liquid is with 37M
3/ h adds I
1Imitate I
1The single-effect evaporator heat exchange area is 380m
2, 1.3 meters of diameters, 5.6 meters of length, tube side is 4 backhauls, works as I
1Imitate the vapour liquid separator liquid level and indicate when reaching total measurement (volume) 3/5, send into I successively
2Imitate II
1Imitate II
2Imitate I
2The single-effect evaporator heat exchange area is 340m
2, 1.1 meters of diameters, 5.2 meters of length, tube side is 4 backhauls, II
1Imitate II
2The single-effect evaporator heat exchange area is 280m
2, 1.5 meters of diameters, 5 meters of length, tube side is 4 backhauls, shell side is 3 backhauls.And make I
2, II
1And II
2When the vapour liquid separator liquid level all is designated as total measurement (volume) 3/5.Control I
2Imitate II
2Imitate 118 ℃ of temperature, 104 ℃ of circulation fluid temperature, I
1Imitate II
1Imitate 82 ℃ of 90 ℃ of circulating temperatures of temperature, internal circulating load 960M
3/ h works as I
1Imitate II
1Imitate pressure and be designated as 0.01Mpa, I
2Imitate II
2When effect pressure is designated as 0.032MPa, from II
2Imitating the finished product discharging opening, can to take out solid content continuously be 39.16% finished product, and flow is 2.13 tons/hour.
Embodiment 2 (independently two imitate vapo(u)rization system, see Fig. 2 for two):
Solid content is that 5.4% clear liquid is with 42M
3The flow of/h adds I respectively
1Imitate and II
1Imitate I
1II
2The single-effect evaporator heat exchange area is 420 square metres, 1.6 meters of diameters, and 6 meters of length, tube side is 6 backhauls, works as I
1Imitate II
1Imitate liquid level and indicate when reaching total measurement (volume) 3/5, send into I respectively
2Imitate II
2Imitate II
1, II
2The single-effect evaporator heat exchange area is 420 square metres, 1.6 meters of diameters, and 6 meters of length, tube side is 6 backhauls, shell side is 3 backhauls control I
2Imitate and II
2Imitating temperature is 76 ℃, 70 ℃ of circulating temperatures, internal circulating load 440M
3/ h, negative pressure indication 0.004MPa is from I
2Imitate and II
2Imitate two discharging openings respectively with 5.67M
3The continuous extraction solid content of the flow of/h is 40% concentrated finished product material.
Embodiment 3 (triple effect evaporation system, i.e. I
1, I
2And II
1Vapo(u)rization system is seen Fig. 1):
Solid content is 4.7% clear liquid, with 45M
3The flow of/h adds I
1Imitate, work as I
1Imitating liquid level indicates when reaching total measurement (volume) 3/5, successively to I
2Effect, II
1Imitate and feed in raw material I
1Imitate I
2Imitate heat exchange area and be 480 square metres, 1.8 meters of diameters, 6.2 meters of length, II
1Imitate II
2Imitate heat exchange area and be 480 square metres, 1.8 meters of diameters, length 6.2 mitron journeys are 8 backhauls, shell side is 4 backhauls, at this moment II
2Be in the cleaning state and stop using, work as I
2, II
1Imitate the liquid level indication and reach at 2/3 o'clock, with II
1Imitate temperature and be controlled at 110 ℃, 96 ℃ of circulation fluid temperature, negative pressure index 0.003Mpa, internal circulating load 920M
3/ h; I
2Imitate temperature and be controlled at 82 ℃, 72 ℃ of circulation fluid temperature, negative pressure index 0.02Mpa, internal circulating load 880M
3/ h, I
1Imitate temperature and be controlled at 55 ℃, 41 ℃ of circulation fluid temperature, negative pressure are 0.04Mpa, and internal circulating load is 550M
3/ h is from II
1Imitate discharging opening with the finished product of 4.98 tons of solid contents 42.5% per hour.
Embodiment 4 (two imitate the level Four production method):
Clear liquid inlet amount 35M
3/ h works as I
1When effect vapour liquid separator liquid level index reached total measurement (volume) 1/2, beginning was to I
2II
1II
2Imitate automatic feed, and make I
2, II
1, II
2The vapour liquid separator liquid level is controlled at total measurement (volume) 1/2.Control I
1, II
1Imitate 85 ℃ of pressure 0.04MPa of temperature, I
2II
2Imitate 62 ℃ of temperature, pressure 0.005Mpa, the level Four internal circulating load is similarly 680M
3/ h is 35% output with 3.2 tons of/hour continuous extraction solid contents at the finished product discharging opening.
Claims (11)
1. method of producing protein feed with the alcohol trough clear liquid, this method comprises: the alcohol trough clear liquid is pumped into I
1Horizontal column tube evaporimeter 3 in, therein through the heating after remove I
1Vapour liquid separator 5 in carry out the negative pressure evaporation enrichment, the liquid material flows out the back circulation from vapour liquid separator 5 and pumps in the above-mentioned horizontal column tube evaporimeter 3, continues to go vapour liquid separator 5 to evaporate enrichment repeatedly after the heating, to finite concentration feed liquid is pumped into I
2Horizontal column tube evaporimeter 7 in, remove I after the heating
2Vapour liquid separator 9, evaporate enrichment once more repeatedly, material is so through I
1, I
2If the evaporation enrichment is from I
2The liquid material that flows out is that to be condensed to solid weight/pasty state fluid gross weight be the pasty state fluid of 35-42.5%, directly sends into drying machine and makes dry powder feeding; If from I
2Liquid material concentration＜35% weight that flows out is passed through II again
1Or II
2Continuous evaporation is sent into drying machine and is made dry powder feeding after being condensed to 35-42.5% weight; Wherein indirect steam that is produced in the drying machine course of work and condensed water are used for as the thermal source in inferior effect evaporation concentration system heating, and the indirect steam that is produced in the work of inferior effect evaporation concentration system is used for the thermal source that heats as preceding effect evaporation concentration system, the vacuum pressure that wherein evaporates in the enrichment system is 0.05-0.003MPa, and the evaporimeter heat source temperature is 38-126 ℃.
2. according to the process of claim 1 wherein the alcohol trough clear liquid is pumped into I simultaneously respectively
1And II
1Two horizontal column tube evaporimeters 3 and 11 in heating and remove to carry out in vapour liquid separator 5 and 13 circular negative-pressure evaporation enrichment respectively, will pump into I from the feed liquid of vapour liquid separator 5 then
2Horizontal column tube evaporimeter 7 heating and remove I
2Vapour liquid separator 9 in negative pressure evaporation concentrate, will pump into II from the feed liquid of vapour liquid separator 13
2Horizontal column tube evaporimeter 15 heating and remove II
2Vapour liquid separator 17 in negative pressure evaporation concentrate, when material is condensed to solid weight/pasty state fluid gross weight respectively and is the pasty state fluid of 35-42.5% in vapour liquid separator 9 and 17 after, directly send into drying machine 23 respectively and make dry powder feeding.
3. according to the method for claim 1 or 2, wherein in inferior effect evaporation concentration system, per hour replenish 2-4 ton primary steam as thermal source.
4. according to the method for claim 1 or 2, it is characterized in that negative pressure system is made up of secondary vacuum jet pump, water ring pump, membrane type tower, water-circulating pump.
5. according to the method for claim 1, it is characterized in that raw material clear liquid concentration is 〉=4% weight.
6. according to the method for claim 2, it is characterized in that raw material clear liquid concentration is lower than 4% weight.
7. according to the method for claim 1 or 2, the internal circulating load that it is characterized in that clear liquid in each single-effect evaporator is 400-1000m
3/ hour.
8. according to the method for claim 1 or 2, it is characterized in that respectively imitating horizontal column tube evaporimeter tube side is the 3-8 backhaul, and shell side is the 2-6 backhaul, and the evaporimeter heat exchange area is 300-800m
2
9. equipment of implementing arbitrary method among the claim 1-8, comprising horizontal column tube evaporimeter (3,7,11,15), vapour liquid separator (5,9,13,17), circulating pump (4,8,12,16), secondary vacuum jet pump (20,21), water ring pump 22, membrane type tower 19 and drying machine is characterized in that this equipment is by following arranged in order:
Isolate the alcohol clear liquid by seperator or settling tank and enter the clear liquid storage tank, squeeze into I with pump
1Circulating pump 4 imports, by circulating pump 4 at I
1Evaporimeter 3 and vapour liquid separator 5 in circulation; The indirect steam that vapour liquid separator 5 evaporates enters vacuum system behind Mo Shi tower 19, the feed liquid that part is concentrated enters I quantitative automaticly
2System is at I
2Evaporimeter 7 and vapour liquid separator 9 in circulate, if from I
2The liquid material that flows out is that to be condensed to solid weight/pasty state fluid gross weight be the pasty state fluid of 35-42.5%, and it automatically sends into drying machine 23 by pump by automatic instrument(s); If from I
2Feed concentration＜35% weight that flows out, then it passes through II again
1Or II
2Continuous evaporation is condensed to and sends into drying machine after the 35-42.5% weight and make dry powder feeding; Wherein indirect steam that is produced in the drying machine course of work and condensed water are used for as the thermal source in inferior effect evaporation concentration system heating, and the indirect steam that is produced in the work of inferior effect evaporation concentration system is used for the thermal source as preceding effect evaporation concentration system.
10. according to the equipment of claim 9, it is characterized in that this equipment is by following arranged in order: the alcohol trough clear liquid is pumped into I simultaneously respectively
1And II
1Two horizontal column tube evaporimeters 3 and 11 in heating and remove to carry out in vapour liquid separator 5 and 13 the circulating and evaporating enrichment respectively, will pump into I from the feed liquid of vapour liquid separator 5 then
2Horizontal column tube evaporimeter 7 heating and remove I
2Vapour liquid separator 9 in negative pressure evaporation concentrate, will pump into II from the feed liquid of vapour liquid separator 13
2Horizontal column tube evaporimeter 15 heating and remove II
2Vapour liquid separator 17 in negative pressure evaporation concentrate, when material is condensed to solid weight/pasty state fluid gross weight respectively and is the pasty state fluid of 35-42.5% in vapour liquid separator 9 and 17 after, directly send into drying machine respectively and make dry powder feeding.
11. according to the equipment of claim 9 or 10, it is characterized in that respectively imitating horizontal column tube evaporimeter tube side is the 3-8 backhaul, shell side is the 2-6 backhaul, and the evaporimeter heat exchange area is 300-800m
2
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97110190A CN1052859C (en) | 1997-07-15 | 1997-07-15 | Method for producing protein feed by using alcoholic grains liquor and equipment thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97110190A CN1052859C (en) | 1997-07-15 | 1997-07-15 | Method for producing protein feed by using alcoholic grains liquor and equipment thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1172594A CN1172594A (en) | 1998-02-11 |
| CN1052859C true CN1052859C (en) | 2000-05-31 |
Family
ID=5171358
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN97110190A Expired - Fee Related CN1052859C (en) | 1997-07-15 | 1997-07-15 | Method for producing protein feed by using alcoholic grains liquor and equipment thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1052859C (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102517340B (en) * | 2011-12-01 | 2013-11-20 | 中石油东北炼化工程有限公司吉林设计院 | Process method for separating and drying lees produced in production process of ethanol with potatoes |
| CN111908691A (en) * | 2020-08-14 | 2020-11-10 | 北京首钢朗泽新能源科技有限公司 | Method and system for co-producing protein powder by evaporation concentration and rectification of fermented liquor |
| CN112843761B (en) * | 2021-03-10 | 2022-08-12 | 郑州博大浓缩干燥设备有限公司 | Lees protein production fodder is with lees filter liquor evaporation concentration system |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1067156A (en) * | 1991-05-28 | 1992-12-23 | 吉林新中国糖厂 | Productive process for making dry-powdered fodder from waste corn fermentation liquor |
| CN1125058A (en) * | 1994-12-22 | 1996-06-26 | 梁兴中 | Method for preparing solid protein feedstuff from sacchariferous fermented waste liquor |
-
1997
- 1997-07-15 CN CN97110190A patent/CN1052859C/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1067156A (en) * | 1991-05-28 | 1992-12-23 | 吉林新中国糖厂 | Productive process for making dry-powdered fodder from waste corn fermentation liquor |
| CN1125058A (en) * | 1994-12-22 | 1996-06-26 | 梁兴中 | Method for preparing solid protein feedstuff from sacchariferous fermented waste liquor |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1172594A (en) | 1998-02-11 |
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