CN212356909U - Fermented mash evaporation concentration and rectification protein powder co-production system - Google Patents
Fermented mash evaporation concentration and rectification protein powder co-production system Download PDFInfo
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- CN212356909U CN212356909U CN202021690389.4U CN202021690389U CN212356909U CN 212356909 U CN212356909 U CN 212356909U CN 202021690389 U CN202021690389 U CN 202021690389U CN 212356909 U CN212356909 U CN 212356909U
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Abstract
The utility model provides a fermented mash evaporative concentration and rectification coproduction albumen powder system, include: an evaporation concentration system, a spray drying system and a rectification dehydration system; the evaporation concentration system is used for carrying out evaporation concentration on the fermented liquor to obtain evaporation concentrated liquor and evaporation clear liquor, and comprises an evaporation concentration device, an evaporation concentrated liquor storage tank and an evaporation clear liquor storage tank, wherein the evaporation concentrated liquor storage tank and the evaporation clear liquor storage tank are both communicated with the evaporation concentration device; the spray drying system is used for carrying out spray drying on the evaporation concentrated solution to obtain protein powder; the rectification dehydration system is used for distilling and dehydrating the membrane filtration clear liquid and the evaporation clear liquid to obtain an ethanol product; according to the invention, the evaporation concentrated solution is directly spray-dried to obtain the protein powder, the evaporation clear solution and the membrane filtration clear solution are jointly rectified and dehydrated to obtain the ethanol product, the protein powder yield is high, the water content of the ethanol product is less than 0.8%, the equipment system cannot be blocked, and the difficulty in protein sewage treatment is reduced.
Description
Technical Field
The utility model relates to a technical field is retrieved to albumen powder, in particular to fermentation mash evaporative concentration and rectification coproduction albumen powder system.
Background
Adopting CO and CO in converter gas of steel plant, metallurgical tail gas and tail gas of petroleum refining2The method for preparing ethanol by adopting microbial fermentation method by using the gases as carbon source is a new technology researched and developed in recent years. At present, the method treats tail gas, synthesis gas, refining tail gas and the like containing CO/CO in the steel industry by a microbial fermentation method2/H2The process for preparing fuel ethanol by using the gas has better development in safety and high efficiency due to the reduction of energy consumption. In the process of producing alcohol by fermenting industrial tail gas, alcohol is extracted by distillationThe solid content in the fermentation waste liquid after ethanol extraction is only mycoprotein, the application value is high, and the direct discharge can greatly increase the sewage load. In the process, the final product comprises raw material ethanol and a large amount of bacteria with the end of life cycle generated in the microbial fermentation process and after the fermentation is finished, the bacteria with the end of life cycle form high-concentration protein wastewater, the concentration of the protein wastewater can reach 25-30 g/L, large-yield protein powder can be collected through recovery treatment, the economic benefit is good, if the protein is directly discharged, the loss of protein substances is finished, and high-concentration protein water can also cause certain influence on the environment.
The existing protein powder extraction method generally comprises the following steps: the process of rectification dehydration → centrifugal separation → spray drying has the technical problems of tower blockage and heat exchange equipment, incomplete centrifugal separation, increased difficulty in protein-containing sewage treatment and the like, brings certain difficulties to system stable operation, sewage treatment and the like, and also causes the loss of the yield of protein powder products.
Therefore, how to develop a protein powder recovery system which has high protein powder yield, does not block an equipment system and greatly reduces the difficulty of protein sewage treatment becomes a technical problem to be solved urgently.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a fermented liquor evaporative concentration and rectification coproduction albumen powder system obtains albumen powder with the direct spray drying of the evaporative concentration liquid that obtains, and the evaporation clear liquid and the membrane filtration clear liquid that obtain carry out the rectification jointly and dewater and obtain the ethanol product, the albumen powder yield is high, the water content of ethanol product < 0.8%, and can not block up equipment system, the albumen sewage treatment degree of difficulty greatly reduced.
In order to achieve the above object, the utility model provides a system of fermentation mash evaporative concentration and rectification coproduction albumen powder, include: an evaporation concentration system, a spray drying system and a rectification dehydration system;
the evaporation concentration system comprises: the device is used for carrying out evaporation concentration on fermented liquor to obtain evaporation concentrated liquor and evaporation clear liquor, and comprises an evaporation concentration device, an evaporation concentrated liquor storage tank and an evaporation clear liquor storage tank, wherein the evaporation concentrated liquor storage tank and the evaporation clear liquor storage tank are communicated with the evaporation concentration device;
the spray drying system is communicated with the evaporation concentrated solution storage tank and is used for carrying out spray drying on the evaporation concentrated solution to obtain protein powder;
and the rectification dehydration system is communicated with the evaporation clear liquid storage tank and is used for distilling and dehydrating the membrane filtration clear liquid and the evaporation clear liquid to obtain an ethanol product.
Further, the evaporation concentration device comprises a single-effect evaporation device or a multi-effect evaporation device.
Further, the evaporation concentration apparatus includes: the system comprises a first evaporation concentration device, a second evaporation concentration device, a third evaporation concentration device, a terminal condenser, a terminal separator and a vacuum pump;
the first evaporation concentration device comprises a first-effect preheater, a first-effect evaporator, a first-effect separator and a first-effect circulating pump;
the primary preheater is used for heating the fermented mash to obtain preheated fermented mash;
the first-effect evaporator comprises a first liquid inlet of the first-effect evaporator, a first steam inlet of the first-effect evaporator, a second liquid inlet of the first-effect evaporator, a first liquid outlet of the first-effect evaporator and a second liquid outlet of the first-effect evaporator, wherein the second liquid inlet of the first-effect evaporator is positioned at the top of the first-effect evaporator, the first liquid inlet of the first-effect evaporator is communicated with the outlet of the first-effect preheater, and the first steam inlet of the first-effect evaporator is used for introducing steam as a heat source;
the first-effect separator comprises a first-effect separator liquid inlet, a first-effect separator liquid outlet and a first-effect separator steam outlet, and the first-effect separator liquid inlet is communicated with the first-effect evaporator second liquid outlet;
the first-effect circulating pump comprises a first-effect circulating pump inlet, a first-effect circulating pump first outlet and a first-effect circulating pump second outlet, the first-effect evaporator first liquid outlet and the first-effect separator liquid outlet are communicated with the first-effect circulating pump inlet, and the first-effect circulating pump first outlet is communicated with the first-effect evaporator second liquid inlet;
the second evaporation and concentration device comprises a double-effect evaporator, a double-effect separator, a double-effect circulating pump and a double-effect clear liquid tank;
the second-effect evaporator comprises a second-effect evaporator first liquid inlet, a second-effect evaporator first steam inlet, a second-effect evaporator second liquid inlet positioned at the top, a second-effect evaporator first liquid outlet positioned at the bottom, a second-effect evaporator second liquid outlet and a second-effect clear liquid outlet, wherein the second-effect evaporator first liquid inlet is communicated with the first-effect circulating pump second outlet, and the second-effect evaporator first steam inlet is communicated with the first-effect separator steam outlet;
the secondary effect separator comprises a secondary effect separator liquid inlet, a secondary effect separator liquid outlet and a secondary effect separator steam outlet, and the secondary effect separator liquid inlet is communicated with the secondary effect evaporator second liquid outlet;
the second-effect circulating pump comprises a second-effect circulating pump inlet, a first second-effect circulating pump outlet and a second-effect circulating pump outlet, the first liquid outlet of the second-effect evaporator and the liquid outlet of the second-effect separator are communicated with the second-effect circulating pump inlet, and the first liquid outlet of the second-effect circulating pump is communicated with the second liquid inlet of the second-effect evaporator;
the double-effect clear liquid tank comprises a double-effect clear liquid tank inlet and a double-effect clear liquid tank outlet, and the double-effect clear liquid tank inlet is communicated with the double-effect clear liquid outlet;
the third evaporation and concentration device comprises a three-effect evaporator, a three-effect separator and a three-effect circulating pump;
the triple-effect evaporator comprises a triple-effect evaporator first liquid inlet, a triple-effect evaporator first steam inlet, a triple-effect evaporator second liquid inlet, a triple-effect evaporator liquid outlet and an evaporation concentrated liquid outlet, wherein the triple-effect evaporator second liquid inlet is communicated with the second outlet of the secondary-effect circulating pump, the triple-effect evaporator first liquid inlet is communicated with the outlet of the secondary-effect clear liquid tank, the triple-effect evaporator first steam inlet is communicated with the steam outlet of the secondary-effect separator, and the evaporation concentrated liquid outlet is communicated with the evaporation concentrated liquid storage tank;
the triple-effect separator comprises a triple-effect separator liquid inlet, a triple-effect separator liquid outlet, an evaporated clear liquid outlet and a triple-effect separator steam outlet, the triple-effect separator liquid inlet is communicated with the triple-effect evaporator liquid outlet, and the evaporated clear liquid outlet is communicated with the evaporated clear liquid storage tank;
the three-effect circulating pump comprises a three-effect circulating pump outlet, a first three-effect circulating pump inlet and a second three-effect circulating pump inlet, and the three-effect circulating pump outlet is communicated with the first liquid inlet of the three-effect evaporator; the first inlet of the three-effect circulating pump is communicated with the second outlet of the two-effect circulating pump, and the second inlet of the three-effect circulating pump is communicated with the liquid outlet of the three-effect separator;
the terminal condenser comprises a terminal condenser inlet, a cooling water inlet, a terminal condenser first liquid outlet and a terminal condenser second liquid outlet, the terminal condenser inlet is communicated with the steam outlet of the triple effect separator, the terminal condenser first liquid outlet is communicated with the evaporation clear liquid storage tank, the terminal condenser second liquid outlet is communicated with the terminal separator inlet, and the vacuum pump is communicated with the terminal separator outlet.
Further, the rectification dehydration system comprises a primary rectification device or a multi-rectification device.
Further, the rectification dehydration system comprises: the system comprises a crude distillation tower, a first rectifying tower, a second rectifying tower and an adsorber;
the crude distillation tower comprises an evaporation clear liquid inlet, an ethanol steam outlet and a crude distillation tower clear liquid outlet, and the evaporation clear liquid inlet is communicated with the evaporation clear liquid storage tank;
the first rectifying tower comprises an ethanol steam inlet, a light wine inlet containing fusel and an ethanol clear liquid outlet, and the ethanol steam inlet is communicated with the ethanol steam outlet of the crude distillation tower;
the second rectifying tower comprises a rectifying clear liquid inlet, a fusel alcohol-containing light wine outlet, an ethanol-containing clear liquid inlet and a semi-finished product ethanol outlet, the rectifying clear liquid inlet is communicated with the crude distillation tower clear liquid outlet, and the fusel alcohol-containing light wine outlet is communicated with the fusel alcohol-containing light wine inlet of the first rectifying tower; the ethanol-containing clear liquid inlet is communicated with the ethanol-containing clear liquid outlet of the first rectifying tower;
the adsorber comprises an adsorber inlet and an adsorber outlet, the adsorber inlet is communicated with the semi-finished product ethanol outlet, and the adsorber outlet is used for outputting ethanol products.
Further, the spray drying system includes the spray drying tower, the spray drying tower includes spray drying tower entry and spray drying tower export, the spray drying tower entry with the evaporation concentrate storage tank is linked together, the spray drying tower export is used for exporting the albumen powder.
The embodiment of the utility model provides an in one or more technical scheme, following technological effect or advantage have at least:
the utility model provides a pair of fermented mash evaporative concentration and rectification coproduction albumen powder system obtains albumen powder with the direct spray drying of the evaporative concentration liquid that obtains, and the evaporation clear liquid and the membrane filtration clear liquid that obtain carry out the rectification jointly and dewater and obtain the ethanol product, the albumen powder yield is high, the water content of ethanol product < 0.8%, and can not block up equipment system, the albumen sewage treatment degree of difficulty greatly reduced.
Drawings
In order to more clearly illustrate the technical solutions in the embodiments of the present invention, the drawings required to be used in the description of the embodiments are briefly introduced below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
FIG. 1 is a flow chart of a system for evaporation concentration and rectification of fermented mash to co-produce protein powder;
FIG. 2 is a structural diagram of a system for evaporation concentration and rectification of fermented mash to co-produce protein powder;
1. an evaporative concentration system; 11. an evaporation concentration device;
111. a first evaporative concentration unit; 1111. a primary preheater; 1112. a first-effect evaporator; 1A, a first liquid inlet of a first-effect evaporator; 1B, a first steam inlet of the first-effect evaporator; 1C, a second liquid inlet of the first-effect evaporator; 1D, a first liquid outlet of the first-effect evaporator; 1E, a second liquid outlet of the first-effect evaporator; 1113. carrying out primary effect separation; 1F, a liquid inlet of the single-effect separator; 1G, a liquid outlet of the single-effect separator; 1H, a steam outlet of the single-effect separator; 1114. a one-effect circulation pump; 1I, an inlet of a one-effect circulating pump; 1J, a first outlet of a first-effect circulating pump; 1K, a second outlet of the first-effect circulating pump;
112. a second evaporative concentration unit; 1121. a second effect evaporator; 2A, a first liquid inlet of a double-effect evaporator; 2B, a first steam inlet of the second-effect evaporator; 2C, a second liquid inlet of the second-effect evaporator; 2D, a first liquid outlet of the second-effect evaporator; 2E, a second liquid outlet of the second-effect evaporator; 2F, a secondary clear liquid outlet; 1122. a two-effect separator; 2G, a liquid inlet of the two-effect separator; 2H, a liquid outlet of the two-effect separator; 2I, a steam outlet of the two-effect separator; 1123. a two-effect circulating pump; 2J, an inlet of a two-effect circulating pump; 2K, a first outlet of the two-effect circulating pump; 2L, a second outlet of the two-effect circulating pump; 1124. a two-effect clear liquid tank;
113. a third evaporation and concentration device; 1131. a triple effect evaporator; 3A, a first liquid inlet of the triple effect evaporator; 3B, a first steam inlet of the triple-effect evaporator; 3C, a second liquid inlet of the triple-effect evaporator; a 3D, triple effect evaporator liquid outlet; 3E, an outlet of the evaporation concentrated solution; 1132. a three-effect separator; 3F, a liquid inlet of the three-effect separator; 3G, a liquid outlet of the three-effect separator; 3H, evaporating a clear liquid outlet; 3I, a steam outlet of the three-effect separator; 1133. a three-effect circulating pump; 3J, discharging a triple-effect circulating pump; 3K, a first inlet of the three-effect circulating pump; 3L, a second inlet of the three-effect circulating pump;
114. a terminal condenser; 4A, a terminal condenser inlet; 4B, a cooling water inlet; 4C, a first liquid outlet of the terminal condenser; 4D, a second liquid outlet of the terminal condenser; 115. a terminal separator; 116. a vacuum pump;
12. a concentrated solution storage tank is evaporated;
13. evaporating the clear liquid storage tank;
2. a spray drying system; 21. a spray drying tower 21; 21A, an inlet 2 of a spray drying tower; 21B, an outlet of a spray drying tower;
3. a rectification dehydration system; 31. a crude distillation column; 5A, a hair clear liquid inlet; 5B, an ethanol steam outlet; 5C, a clear liquid outlet of the crude distillation tower; 32. a first rectification column; 5D, an ethanol steam inlet; 5E, enabling the fusel-containing light wine to enter the mouth; 5F, an outlet for ethanol-containing clear liquid; 33. a second rectification column; 5G, rectifying a clear liquid inlet; 5H, discharging the weak wine containing fusel; 5I, an ethanol-containing clear liquid inlet; 5J, discharging the semi-finished product ethanol; 34. an adsorber; 5K, an absorber inlet; 5L and an adsorber outlet.
Detailed Description
The present invention will be described in detail below with reference to specific embodiments and examples, and the advantages and various effects of the present invention will be more clearly apparent from the description. It will be understood by those skilled in the art that the present embodiments and examples are illustrative of the present invention, and are not to be construed as limiting the invention.
Throughout the specification, unless otherwise specifically noted, terms used herein should be understood as having meanings as commonly used in the art. Accordingly, unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. If there is a conflict, the present specification will control.
Unless otherwise specifically stated, various raw materials, reagents, instruments, systems and the like used in the present invention are commercially available or can be prepared by an existing method.
The embodiment of the utility model provides a technical scheme is for solving above-mentioned technical problem, and the general thinking is as follows:
the embodiment of the utility model provides a still provide a system of fermented mash evaporative concentration and rectification coproduction albumen powder is shown in figure 2, include: an evaporation concentration system 1, a spray drying system 2 and a rectification dehydration system 3;
the evaporation concentration system 1 is used for carrying out evaporation concentration on the fermented liquor to obtain evaporation concentrated liquor and evaporation clear liquor, and comprises an evaporation concentration device 11, an evaporation concentrated liquor storage tank 12 and an evaporation clear liquor storage tank 13, wherein the evaporation concentrated liquor storage tank 12 and the evaporation clear liquor storage tank 13 are both communicated with the evaporation concentration device 11;
the spray drying system 2 is communicated with the evaporation concentrated solution storage tank 12 and is used for carrying out spray drying on the evaporation concentrated solution;
and the rectification dehydration system 3 is communicated with the evaporation clear liquid storage tank 13 and is used for distilling and dehydrating the membrane filtration clear liquid and the evaporation clear liquid to obtain an ethanol product.
The embodiment of the utility model provides a pair of system of fermented mash evaporative concentration and rectification coproduction albumen powder, spray drying system 2 with evaporative concentration liquid storage tank 12 is linked together, rectification dewatering system 3 with evaporation clear solution storage tank 13 is linked together, and the direct spray drying of evaporative concentration liquid that will obtain obtains albumen powder, and the evaporation clear solution and the membrane filtration clear solution that obtain carry out the rectification jointly and dewater and obtain the ethanol product, the albumen powder yield is high, the water content of ethanol product < 0.8%, and can not block up equipment system, albumen sewage treatment degree of difficulty greatly reduced. In the prior art, the concentrated solution and the clear solution are generally led away from a distillation system, and then the protein in the concentrated solution blocks the equipment due to denaturation and precipitation, so that the distillation system is influenced, a large amount of protein powder is lost, the yield of the protein powder is very low, and finally the outputted clear solution contains mycoprotein, so that the water treatment is influenced, and the recovery rate of centrifugal separation is low.
The embodiment of the utility model provides a use flow of system of fermentation mash evaporative concentration and rectification coproduction albumen powder, as shown in figure 1, including following step:
s1, obtaining fermented liquor and membrane filtration clear liquid;
s2, carrying out evaporation concentration on the fermented mash to obtain an evaporation concentrated solution and an evaporation clear solution;
s3, spray drying the evaporated and concentrated solution to obtain protein powder;
s4, rectifying and dehydrating the evaporation clear liquid and the membrane filtration clear liquid to obtain an absolute ethyl alcohol product.
Preferably, the evaporative concentration apparatus 11 comprises a single effect evaporation apparatus or a multiple effect evaporation apparatus.
Preferably, the evaporation concentration apparatus 11 includes: a first, second and third evaporation- concentration devices 111, 112 and 113, a terminal condenser 114, a terminal separator 115 and a vacuum pump 116;
the first evaporation concentration device 111 comprises a one-effect preheater 1111, a one-effect evaporator 1112, a one-effect separator 1113 and a one-effect circulating pump 1114;
the primary preheater 1111 is used for heating fermented mash to obtain preheated fermented mash;
the first-effect evaporator 1112 comprises a first-effect evaporator first liquid inlet 1A, a first-effect evaporator first steam inlet 1B, a first-effect evaporator second liquid inlet 1C positioned at the top, a first-effect evaporator first liquid outlet 1D positioned at the bottom and a first-effect evaporator second liquid outlet 1E, the first-effect evaporator first liquid inlet 1A is communicated with the outlet of the first-effect preheater 1111, and the first-effect evaporator first steam inlet 1B is used for introducing steam as a heat source;
the first-effect separator 1113 comprises a first-effect separator liquid inlet 1F, a first-effect separator liquid outlet 1G and a first-effect separator steam outlet 1H, and the first-effect separator liquid inlet 1F is communicated with the first-effect evaporator second liquid outlet 1E;
the first-effect circulating pump 1114 comprises a first-effect circulating pump inlet 1I, a first-effect circulating pump first outlet 1J and a first-effect circulating pump second outlet 1K, the first-effect evaporator first liquid outlet 1D and the first-effect separator liquid outlet 1G are both communicated with the first-effect circulating pump inlet 1I, and the first-effect circulating pump first outlet 1J is communicated with the first-effect evaporator second liquid inlet 1C;
the second evaporation concentration device 112 comprises a second-effect evaporator 1121, a second-effect separator 1122, a second-effect circulating pump 1123 and a second-effect clear liquid tank 1124;
the second-effect evaporator 1121 comprises a second-effect evaporator first liquid inlet 2A, a second-effect evaporator first vapor inlet 2B, a second-effect evaporator second liquid inlet 2C located at the top, a second-effect evaporator first liquid outlet 2D located at the bottom, a second-effect evaporator second liquid outlet 2E and a second-effect clear liquid outlet 2F, wherein the second-effect evaporator first liquid inlet 2A is communicated with the first-effect circulating pump second outlet 1K, and the second-effect evaporator first vapor inlet 2B is communicated with the first-effect separator vapor outlet 1H;
the double-effect separator 1122 comprises a double-effect separator liquid inlet 2G, a double-effect separator liquid outlet 2H and a double-effect separator vapor outlet 2I, and the double-effect separator liquid inlet 2G is communicated with the second liquid outlet 2E of the double-effect evaporator;
the two-effect circulating pump 1123 comprises a two-effect circulating pump inlet 2J, a two-effect circulating pump first outlet 2K and a two-effect circulating pump second outlet 2L, the two-effect evaporator first liquid outlet 2D and the two-effect separator liquid outlet 2H are both communicated with the two-effect circulating pump inlet 2J, and the two-effect circulating pump first outlet 2K is communicated with the two-effect evaporator second liquid inlet 2C;
the double-effect clear liquid tank 1124 comprises a double-effect clear liquid tank inlet and a double-effect clear liquid tank outlet, the double-effect clear liquid tank inlet is communicated with the double-effect clear liquid outlet 2F, and the double-effect clear liquid tank outlet is communicated with a first liquid inlet of the three-effect evaporator;
the third evaporation concentration device 113 comprises a three-effect evaporator 1131, a three-effect separator 1132 and a three-effect circulating pump 1133;
the triple-effect evaporator 1131 comprises a triple-effect evaporator first liquid inlet 3A, a triple-effect evaporator first steam inlet 3B, a triple-effect evaporator second liquid inlet 3C, a triple-effect evaporator liquid outlet 3D and an evaporation concentrate outlet 3E, wherein the triple-effect evaporator second liquid inlet 3C is communicated with the second outlet 2L of the two-effect circulating pump, the triple-effect evaporator first liquid inlet 3A is communicated with the outlet 2N of the two-effect clear liquid tank, the triple-effect evaporator first steam inlet 3B is communicated with the steam outlet 2I of the two-effect separator, and the evaporation concentrate outlet 3E is communicated with the evaporation concentrate storage tank 12;
the triple-effect separator 1132 comprises a triple-effect separator liquid inlet 3F, a triple-effect separator liquid outlet 3G, an evaporated clear liquid outlet 3H and a triple-effect separator steam outlet 3I, the triple-effect separator liquid inlet 3F is communicated with the triple-effect evaporator liquid outlet 3D, and the evaporated clear liquid outlet 3H is communicated with the evaporated clear liquid storage tank;
the three-effect circulating pump 1133 comprises a three-effect circulating pump outlet 3J, a three-effect circulating pump first inlet 3K and a three-effect circulating pump second inlet 3L, wherein the three-effect circulating pump outlet 3J is communicated with the three-effect evaporator first liquid inlet 3A; the first inlet 3K of the three-effect circulating pump is communicated with the second outlet 2L of the two-effect circulating pump, and the second inlet 3L of the three-effect circulating pump is communicated with the liquid outlet 3G of the three-effect separator;
the terminal condenser 114 comprises a terminal condenser inlet 4A, a cooling water inlet 4B, a terminal condenser first liquid outlet 4C and a terminal condenser second liquid outlet 4D, the terminal condenser inlet 4A is communicated with a steam outlet 3I of the triple effect separator, the terminal condenser first liquid outlet 4C is communicated with the evaporation clear liquid storage tank 13, the terminal condenser second liquid outlet 4D is communicated with an inlet of the terminal separator 115, and the vacuum pump 116 is communicated with an outlet of the terminal separator 115.
As can be seen from the above, the fermented mash enters the first-effect preheater 1111 for preheating to obtain preheated fermented mash, enters the first-effect evaporator 1112 from the port 1A, enters the first-effect evaporator 1112 from the port 1B by using 6-8brag saturated steam as a heat source,
a 2J port of the first-effect circulating pump 1114 is communicated with a 1D port of the first-effect evaporator and a 2H port of the first-effect separator, a 2K port of the first-effect circulating pump is communicated with a 2C port at the top of the first-effect evaporator, so that concentrated liquor in the first-effect evaporator is circularly heated, and fermented liquor is preliminarily concentrated by the first-effect evaporator 1112; the first-effect evaporator 1112 is communicated with the first-effect separator 1113, and is separated in the first-effect separator 1113 to obtain a first-effect evaporation concentrated solution;
the first-effect evaporation concentrated solution is conveyed to a second-effect evaporator 1121 for secondary concentration through a first-effect circulating pump 1114; performing gas-liquid separation by the first-effect separator 1113, and using the generated steam as a heat source of the second-effect evaporator 1121; an inlet of the two-effect circulating pump 1123 is communicated with the bottom of the two-effect evaporator 1121 and the two-effect separator 1122, a port 2K of the two-effect circulating pump is communicated with a port 2C at the top of the two-effect evaporator 1121, and evaporation concentrated solution is circularly heated and concentrated; the second-effect evaporator 1121 is communicated with the second-effect separator 1122, and is separated in the second-effect separator 1122 to obtain a second-effect evaporation concentrated solution;
an outlet of the two-effect circulating pump 1123 is communicated with a three-effect circulating pump 1133, and the two-effect evaporation concentrated solution is conveyed to a three-effect evaporator 1131 for three-time concentration. A port 2I of the two-effect separator is communicated with a port 3B of the three-effect evaporator 1131 and is used as a heat source of the three-effect evaporator 1131; the clear liquid produced by the second-effect evaporator is buffered by a second-effect clear liquid tank 1124 and is used as the other part of heat source of the third-effect evaporator 1131;
the outlet of the triple-effect circulating pump 1133 is communicated with the bottom of the triple-effect evaporator 1131, and the evaporation concentrated solution is circularly heated and concentrated; the triple-effect evaporator 1131 is communicated with a triple-effect separator 1132; the evaporated clear liquid generated by the triple-effect evaporator 1131 is communicated with an evaporated clear liquid storage tank 13, and clear liquid which almost does not contain mycoprotein is conveyed out;
the 3H port of the triple-effect separator is communicated with an evaporation concentrated solution storage tank 12, and evaporation concentrated solution with the concentration of 10-30% and the ethanol content of less than 1g/L is conveyed out;
the gas phase outlet of the triple-effect separator 1132 is communicated with a terminal condenser 114, and the terminal condenser 114 is also communicated with an evaporated clear liquid storage tank 13 to deliver clear liquid which hardly contains mycoprotein; the evaporated clear liquid tank 13 also receives clear liquid from the fermentation after membrane filtration. The evaporation clear liquid storage tank 13 is communicated with the crude distillation tower 31 through a pump, and crude alcohol and water in the evaporation clear liquid are primarily separated.
The terminal condenser 114 is also communicated with a terminal separator 115, and the terminal separator 115 is communicated with a vacuum pump (16) to provide a negative pressure environment for the whole evaporation and concentration system;
preferably, the rectifying and dewatering system 3 comprises a primary rectifying device or a multi-rectifying device.
Preferably, the rectifying and dehydrating system 3 comprises: a crude distillation tower 31, a first rectifying tower 32, a second rectifying tower 33 and an adsorber 34;
the crude distillation tower 31 comprises an evaporation clear liquid inlet 5A, an ethanol steam outlet 5B and a crude distillation tower clear liquid outlet 5C, wherein the evaporation clear liquid inlet 5A is communicated with the evaporation clear liquid storage tank 13;
the first rectifying tower 32 comprises an ethanol steam inlet 5D, a fusel-containing light wine inlet 5E and an ethanol clear liquid outlet 5F, wherein the ethanol steam inlet 5D is communicated with the crude distillation tower ethanol steam outlet 5B;
the second rectifying tower 33 comprises a rectifying clear liquid inlet 5G, a fusel alcohol-containing light wine outlet 5H, an ethanol-containing clear liquid inlet 5I and a semi-finished product ethanol outlet 5J, wherein the rectifying clear liquid inlet 5G is communicated with the crude distillation tower clear liquid outlet 5C, and the fusel alcohol-containing light wine outlet 5H is communicated with the fusel alcohol-containing light wine inlet 5E of the first rectifying tower; the ethanol-containing clear liquid inlet 5I is communicated with the ethanol-containing clear liquid outlet 5F of the first rectifying tower;
the adsorber 34 comprises an adsorber inlet 5K and an adsorber outlet 5L, the adsorber inlet 5K is communicated with the semi-finished product ethanol outlet 5J, and the adsorber outlet 5L is used for outputting ethanol products.
From the above, the first rectifying tower 32 is communicated with the outlet 5B at the top of the crude distillation tower 31, the first rectifying tower 32 is also communicated with the middle upper part of the second rectifying tower 33, and receives a part of the light wine containing fusel alcohol in the second rectifying tower 33; a part of the ethanol-containing clear liquid in the crude distillation tower 31 is conveyed to a second rectifying tower 33; ethanol with the concentration of about 95% is extracted from the side of the first rectifying tower 32 and is conveyed to the upper part of the second rectifying tower 33, and semi-finished ethanol with the concentration of more than or equal to 95% is output from the top of the second rectifying tower 33 to the adsorber 34; most of the water in the semi-finished product ethanol is removed by the absorber 34, and the final product is an absolute ethanol product with the water content less than 0.8 percent.
Preferably, the spray drying system 2 comprises a spray drying tower 21, the spray drying tower 21 comprises a spray drying tower inlet 21A and a spray drying tower outlet 21B, the spray drying tower inlet 21A is communicated with the evaporation concentrate storage tank 12, and the spray drying tower outlet 21B is used for outputting protein powder.
Preferably, the system for the evaporative concentration and rectification of the fermented mash to co-produce the protein powder further comprises a membrane filtration system, wherein the membrane filtration system is used for carrying out membrane filtration on the fermented waste liquid to obtain the fermented mash and a membrane filtration clear liquid.
The system for evaporative concentration and rectification of fermented mash and co-production of protein powder is described in detail below with reference to examples, comparative examples and experimental data.
Example 1
S1, obtaining fermented liquor and membrane filtration clear liquid;
s2, introducing the fermented mash into an evaporation concentration system 1 for carrying out evaporation concentration on the fermented mash to obtain an evaporation concentrated solution and an evaporation clear solution, introducing the evaporation concentrated solution into an evaporation concentrated solution storage tank 12, and introducing the obtained evaporation clear solution into an evaporation clear solution storage tank 13; the evaporation concentration system adopts 0.6-0.8mpa saturated steam, the temperature of the evaporation concentration system is less than or equal to 65 ℃, and the ethanol yield of the evaporation concentration liquid is less than 0.08 percent.
S3, the evaporation concentrated solution storage tank 12 is communicated with a spray drying system 2 and is used for carrying out spray drying on the evaporation concentrated solution to obtain protein powder; the heat source of the spray drying tower adopts 0.6-0.8mpa saturated steam, the air inlet temperature is controlled to be less than 180 ℃, and the air exhaust temperature of the drying tower is controlled to be 65-85 ℃.
S4, the evaporation clear liquid storage tank 13 is communicated with the rectification dehydration system 3 and is used for carrying out distillation dehydration on the membrane filtration clear liquid and the evaporation clear liquid to obtain an ethanol product; the rectification heat source adopts 0.6-0.8mpa saturated steam, the temperature at the bottom of the coarse distillation tower in the system is controlled to be less than 85 ℃, and the water content of the product ethanol is controlled to be less than 0.8%.
Comparative example 1
In this comparative example, the concentrate and the clear solution were taken together in a distillation system.
S1, obtaining fermented liquor and membrane filtration clear liquid;
s2, feeding fermented mash into a rectifying system coarse distillation tower, feeding membrane-filtered clear liquid into a rectifying system No. 2 rectifying tower, feeding 95% ethanol produced by the rectifying tower No. 2 into a molecular sieve dehydrator, and feeding the final product of the rectifying dehydration system into absolute ethanol with the water content of less than 0.8%;
s3, separating the residual distilled water in the bottom of the crude distillation tower by a centrifuge, and feeding the centrifugal clear liquid into a sewage treatment system
S4, spray drying the concentrated solution produced by the centrifuge to obtain the final product of protein powder.
Test example 1
The yield of protein powder obtained in each example and comparative example, the water content of the obtained ethanol product, the recovery rate of centrifugal separation of protein powder, and the blockage of the distillation system were calculated and shown in Table 1.
TABLE 1
From the data in table 1, it can be seen that:
in comparative example 1, the concentrated solution and the clear solution are fed into a distillation system together, the yield of the protein powder is only 70-80%, the alcohol content of the distilled water at the bottom of the tower is less than 0.08%, a centrifugal separation system is needed to be arranged behind the distillation system to concentrate the mycoprotein, the recovery rate of the centrifugal separation is low, and the blockage of the distillation system is serious.
To sum up, the utility model provides a pair of fermented mash evaporative concentration and rectification coproduction albumen powder system, the direct spray drying of the evaporative concentration liquid that will obtain obtains albumen powder, and the evaporation clear solution and the membrane filtration clear solution that obtain carry out the rectification jointly and dewater and obtain the ethanol product, albumen powder yield is high, does not influence ethanol comprehensive recovery rate, and can not block up equipment system, albumen sewage treatment degree of difficulty greatly reduced.
Finally, it should also be noted that the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or system that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or system.
While the preferred embodiments of the present invention have been described, additional variations and modifications in those embodiments may occur to those skilled in the art once they learn of the basic inventive concepts. It is therefore intended that the appended claims be interpreted as including the preferred embodiment and all such alterations and modifications as fall within the scope of the invention.
It will be apparent to those skilled in the art that various changes and modifications may be made without departing from the spirit and scope of the invention. Thus, if such modifications and variations of the present invention fall within the scope of the claims and their equivalents, the present invention is also intended to include such modifications and variations.
Claims (8)
1. The utility model provides a fermented mash evaporation concentration and rectification coproduction albumen powder system which characterized in that includes: an evaporation concentration system, a spray drying system and a rectification dehydration system;
the evaporation concentration system is used for carrying out evaporation concentration on the fermented liquor to obtain evaporation concentrated liquor and evaporation clear liquor, and comprises an evaporation concentration device, an evaporation concentrated liquor storage tank and an evaporation clear liquor storage tank, wherein the evaporation concentrated liquor storage tank and the evaporation clear liquor storage tank are both communicated with the evaporation concentration device;
the spray drying system is communicated with the evaporation concentrated solution storage tank and is used for carrying out spray drying on the evaporation concentrated solution to obtain protein powder;
and the rectification dehydration system is communicated with the evaporation clear liquid storage tank and is used for distilling and dehydrating the membrane filtration clear liquid and the evaporation clear liquid to obtain an ethanol product.
2. The system for evaporative concentration and rectification of protein powder produced from fermented mash according to claim 1, wherein the evaporative concentration device comprises a single-effect evaporation device or a multi-effect evaporation device.
3. The system for evaporative concentration and rectification of protein powder co-production of fermented mash according to claim 1 or 2, wherein the evaporative concentration device comprises: the system comprises a first evaporation concentration device, a second evaporation concentration device, a third evaporation concentration device, a terminal condenser, a terminal separator and a vacuum pump;
the first evaporation concentration device comprises a first-effect preheater, a first-effect evaporator, a first-effect separator and a first-effect circulating pump;
the primary preheater is used for heating the fermented mash to obtain preheated fermented mash;
the first-effect evaporator comprises a first liquid inlet of the first-effect evaporator, a first steam inlet of the first-effect evaporator, a second liquid inlet of the first-effect evaporator, a first liquid outlet of the first-effect evaporator and a second liquid outlet of the first-effect evaporator, wherein the second liquid inlet of the first-effect evaporator is positioned at the top of the first-effect evaporator, the first liquid inlet of the first-effect evaporator is communicated with the outlet of the first-effect preheater, and the first steam inlet of the first-effect evaporator is used for introducing steam as a heat source;
the first-effect separator comprises a first-effect separator liquid inlet, a first-effect separator liquid outlet and a first-effect separator steam outlet, and the first-effect separator liquid inlet is communicated with the first-effect evaporator second liquid outlet;
the first-effect circulating pump comprises a first-effect circulating pump inlet, a first-effect circulating pump first outlet and a first-effect circulating pump second outlet, the first-effect evaporator first liquid outlet and the first-effect separator liquid outlet are communicated with the first-effect circulating pump inlet, and the first-effect circulating pump first outlet is communicated with the first-effect evaporator second liquid inlet;
the second evaporation and concentration device comprises a double-effect evaporator, a double-effect separator, a double-effect circulating pump and a double-effect clear liquid tank;
the second-effect evaporator comprises a second-effect evaporator first liquid inlet, a second-effect evaporator first steam inlet, a second-effect evaporator second liquid inlet positioned at the top, a second-effect evaporator first liquid outlet positioned at the bottom, a second-effect evaporator second liquid outlet and a second-effect clear liquid outlet, wherein the second-effect evaporator first liquid inlet is communicated with the first-effect circulating pump second outlet, and the second-effect evaporator first steam inlet is communicated with the first-effect separator steam outlet;
the secondary effect separator comprises a secondary effect separator liquid inlet, a secondary effect separator liquid outlet and a secondary effect separator steam outlet, and the secondary effect separator liquid inlet is communicated with the secondary effect evaporator second liquid outlet;
the second-effect circulating pump comprises a second-effect circulating pump inlet, a first second-effect circulating pump outlet and a second-effect circulating pump outlet, the first liquid outlet of the second-effect evaporator and the liquid outlet of the second-effect separator are communicated with the second-effect circulating pump inlet, and the first liquid outlet of the second-effect circulating pump is communicated with the second liquid inlet of the second-effect evaporator;
the double-effect clear liquid tank comprises a double-effect clear liquid tank inlet and a double-effect clear liquid tank outlet, and the double-effect clear liquid tank inlet is communicated with the double-effect clear liquid outlet;
the third evaporation and concentration device comprises a three-effect evaporator, a three-effect separator and a three-effect circulating pump;
the triple-effect evaporator comprises a triple-effect evaporator first liquid inlet, a triple-effect evaporator first steam inlet, a triple-effect evaporator second liquid inlet, a triple-effect evaporator liquid outlet and an evaporation concentrated liquid outlet, wherein the triple-effect evaporator second liquid inlet is communicated with the second outlet of the secondary-effect circulating pump, the triple-effect evaporator first liquid inlet is communicated with the outlet of the secondary-effect clear liquid tank, the triple-effect evaporator first steam inlet is communicated with the steam outlet of the secondary-effect separator, and the evaporation concentrated liquid outlet is communicated with the evaporation concentrated liquid storage tank;
the triple-effect separator comprises a triple-effect separator liquid inlet, a triple-effect separator liquid outlet, an evaporated clear liquid outlet and a triple-effect separator steam outlet, the triple-effect separator liquid inlet is communicated with the triple-effect evaporator liquid outlet, and the evaporated clear liquid outlet is communicated with the evaporated clear liquid storage tank;
the three-effect circulating pump comprises a three-effect circulating pump outlet, a first three-effect circulating pump inlet and a second three-effect circulating pump inlet, and the three-effect circulating pump outlet is communicated with the first liquid inlet of the three-effect evaporator; the first inlet of the three-effect circulating pump is communicated with the second outlet of the two-effect circulating pump, and the second inlet of the three-effect circulating pump is communicated with the liquid outlet of the three-effect separator;
the terminal condenser comprises a terminal condenser inlet, a cooling water inlet, a terminal condenser first liquid outlet and a terminal condenser second liquid outlet, the terminal condenser inlet is communicated with the steam outlet of the triple effect separator, the terminal condenser first liquid outlet is communicated with the evaporation clear liquid storage tank, the terminal condenser second liquid outlet is communicated with the terminal separator inlet, and the vacuum pump is communicated with the terminal separator outlet.
4. The system for evaporative concentration and rectification of fermented liquor and co-production of protein powder according to claim 1, wherein the rectification dehydration system comprises a primary rectification device or a multi-rectification device.
5. The system for evaporative concentration and rectification of protein powder co-production of fermented mash according to claim 1 or 4, wherein the rectification dehydration system comprises: the system comprises a crude distillation tower, a first rectifying tower, a second rectifying tower and an adsorber;
the crude distillation tower comprises an evaporation clear liquid inlet, an ethanol steam outlet and a crude distillation tower clear liquid outlet, and the evaporation clear liquid inlet is communicated with the evaporation clear liquid storage tank;
the first rectifying tower comprises an ethanol steam inlet, a light wine inlet containing fusel and an ethanol clear liquid outlet, and the ethanol steam inlet is communicated with the ethanol steam outlet of the crude distillation tower;
the second rectifying tower comprises a rectifying clear liquid inlet, a fusel alcohol-containing light wine outlet, an ethanol-containing clear liquid inlet and a semi-finished product ethanol outlet, the rectifying clear liquid inlet is communicated with the crude distillation tower clear liquid outlet, and the fusel alcohol-containing light wine outlet is communicated with the fusel alcohol-containing light wine inlet of the first rectifying tower; the ethanol-containing clear liquid inlet is communicated with the ethanol-containing clear liquid outlet of the first rectifying tower;
the adsorber comprises an adsorber inlet and an adsorber outlet, the adsorber inlet is communicated with the semi-finished product ethanol outlet, and the adsorber outlet is used for outputting ethanol products.
6. The system for evaporative concentration and rectification of protein powder produced from fermented mash according to claim 1, wherein the spray drying system comprises a spray drying tower, the spray drying tower comprises a spray drying tower inlet and a spray drying tower outlet, the spray drying tower inlet is communicated with the evaporative concentrate storage tank, and the spray drying tower outlet is used for outputting protein powder.
7. The system for the evaporative concentration and rectification of fermented liquor and the co-production of protein powder according to claim 1, wherein the system for the evaporative concentration and rectification of fermented liquor and the co-production of protein powder further comprises a membrane filtration system, wherein the membrane filtration system is used for performing membrane filtration on fermented waste liquid to obtain fermented liquor and membrane filtration clear liquid.
8. The system for the evaporative concentration and rectification of fermented mash and co-production of protein powder according to claim 1, wherein the evaporated clear liquid storage tank is provided with a membrane filtered clear liquid inlet for receiving membrane filtered clear liquid.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| 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 |
| CN112843761A (en) * | 2021-03-10 | 2021-05-28 | 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 |
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2020
- 2020-08-14 CN CN202021690389.4U patent/CN212356909U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN112843761A (en) * | 2021-03-10 | 2021-05-28 | 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 |
| 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 |
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Address after: Room 1601-6, 16th floor, building 1, yard 1, tianshunzhuang North Road, Shijingshan District, Beijing 100043 Patentee after: Beijing Shougang langze Technology Co.,Ltd. Patentee after: HEBEI SHOULANG NEW ENERGY TECHNOLOGY CO.,LTD. Patentee after: Beijing Shoulang Biotechnology Co.,Ltd. Address before: 100043 room 1601-6, building 1, yard 1, tianshunzhuang North Road, Shijingshan District, Beijing Patentee before: BEIJING SHOUGANG LANGZE NEW ENERGY TECHNOLOGY CO.,LTD. Patentee before: HEBEI SHOULANG NEW ENERGY TECHNOLOGY CO.,LTD. Patentee before: Beijing Shoulang Biotechnology Co.,Ltd. |