CN111908691A - Method and system for co-producing protein powder by evaporation concentration and rectification of fermented liquor - Google Patents

Abstract

The invention discloses a method for co-producing protein powder by evaporating, concentrating and rectifying fermentation mash, comprising: obtaining a fermented mature mash, and subjecting the fermented mature mash to membrane filtration to obtain a fermented mash and a membrane-filtered clear liquid; Evaporating and concentrating the fermented mash to obtain an evaporating concentrate and an evaporating clear liquid; subjecting the evaporating concentrate to spray drying to obtain protein powder; subjecting the evaporating clear liquid and the membrane filtration clear liquid to rectification and dehydration , to obtain anhydrous ethanol products. The invention provides a system for co-producing protein powder by evaporation concentration and rectification of fermented mash, including: an evaporation concentration system, a spray drying system and a rectification dehydration system; the obtained evaporation concentrate is directly spray-dried to obtain protein powder, The obtained evaporative clear liquid and membrane filtration clear liquid are jointly rectified and dehydrated to obtain anhydrous ethanol product, the protein powder has a high yield, does not affect the ethanol recovery rate, does not block equipment systems, and greatly reduces the difficulty of sewage treatment.

Description

A method and system for co-producing protein powder by evaporating, concentrating and rectifying fermentation mash

technical field

The invention relates to the technical field of ethanol production by gas fermentation and protein powder recovery, in particular to a method and system for co-producing protein powder by evaporating, concentrating and rectifying fermentation mash.

Background technique

The use of CO and CO ₂ and other gases in the converter gas, metallurgical tail gas and petroleum refining tail gas as the carbon source, and the use of microbial fermentation to produce ethanol is a new technology researched and developed in recent years. At present, the process of preparing fuel ethanol by treating iron and steel industry tail gas, synthesis gas, refining tail gas and other gases containing CO/CO ₂ /H ₂ by microbial fermentation method has been developed safely and efficiently because it reduces energy consumption. In the process of producing alcohol by fermentation of industrial tail gas, the solid content in the fermentation mash after ethanol extraction by rectification is only bacterial protein, which has high application value, while direct discharge will greatly increase the sewage load. In this process, in addition to the raw material ethanol, the final product also contains a large number of bacteria at the end of the life cycle produced during the microbial fermentation process and after the fermentation is completed. These bacteria at the end of the life cycle form high-concentration protein wastewater, the concentration of which can be As high as 25-30g/L, if it is recycled, it can also collect a large amount of protein powder, which has good economic benefits. If it is directly discharged, it will not only complete the loss of protein substances, but also high-concentration protein water will also cause certain damage to the environment. Impact.

The existing protein powder extraction method is usually: rectification dehydration → centrifugal separation → spray drying process, there are technical problems such as clogging of towers and heat exchange equipment, incomplete centrifugal separation, and increased difficulty in treating protein-containing sewage. Stable operation, sewage treatment, etc. have brought certain problems, and also caused the loss of protein powder product output.

Therefore, how to develop a method and system for recovering protein powder with high protein powder yield, without clogging the equipment system and greatly reducing the difficulty of protein sewage treatment has become an urgent technical problem to be solved.

SUMMARY OF THE INVENTION

The purpose of the present invention is to provide a method and system for co-producing protein powder by evaporation, concentration and rectification of fermented mash. The ethanol product is obtained by distillation and dehydration, the protein powder yield is high, the recovery rate of the ethanol product is not affected, the equipment system is not blocked, and the difficulty of protein sewage treatment is greatly reduced.

In order to achieve the above object, the present invention provides a method for co-producing protein powder by evaporation, concentration and rectification of fermented mash, the method comprising:

Obtaining fermented mature mash, carrying out membrane filtration on the fermented mature mash to obtain fermentation mash and membrane filtration clear liquid;

Evaporating and concentrating the fermented mash to obtain an evaporating concentrate and an evaporating clear liquid;

The evaporative concentrate is spray-dried to obtain protein powder;

The evaporation clear liquid and the membrane filtration clear liquid are subjected to rectification and dehydration to obtain an ethanol product.

Further, the conditions for the evaporative concentration are as follows: the evaporative concentration temperature is controlled at 45°C to 65°C, the concentration of solids after concentration is 10% to 30%, and the ethanol content in the evaporative concentrate is less than 0.08%.

Further, the conditions of the spray drying are as follows: the inlet temperature of the hot air is 150°C to 210°C, the outlet temperature is 65°C to 85°C, and the temperature of the feed liquid is 35°C to 80°C.

Further, during the rectification and dehydration, the temperature of the bottom of the crude distillation tower is less than 85°C, and the water content of the anhydrous ethanol product is less than 0.8%.

The invention provides a system for co-producing protein powder by evaporation concentration and rectification of fermented mash, including an evaporation concentration system, a spray drying system and a rectification dehydration system;

The evaporative concentration system: used for evaporating and concentrating the fermented mash to obtain an evaporating concentrate and an evaporating clear liquid, including an evaporating and concentrating device, an evaporating and concentrating liquid storage tank and an evaporating clear liquid storage tank, the evaporating and concentrated liquid storage tank and The evaporative clear liquid storage tanks are all communicated with the evaporative concentration device;

The spray drying system is communicated with the evaporative concentrate storage tank for spray drying the evaporative concentrate to obtain protein powder;

The rectification and dehydration system is communicated with the evaporative clear liquid storage tank, and is used for rectifying and dehydrating the membrane filtration clear liquid and the evaporative clear liquid to obtain anhydrous ethanol product.

Further, the evaporation and concentration device includes a single-effect evaporation device or a multi-effect evaporation device.

Further, the evaporative concentration device includes: a first evaporative concentration device, a second evaporative concentration device and a third evaporative concentration device, a terminal condenser, a terminal separator and a vacuum pump;

The first evaporation and concentration device includes a first-effect preheater, a first-effect evaporator, a first-effect separator and a first-effect circulating pump;

The first-effect preheater is used for heating fermentation mash to obtain preheated fermentation mash;

The first-effect evaporator includes a first liquid inlet of the first-effect evaporator, a first vapor inlet of the first-effect evaporator, a second liquid inlet of the first-effect evaporator at the top, a first liquid outlet of the first-effect evaporator at the bottom, and a first-effect evaporator at the bottom. The second liquid outlet 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 vapor outlet, and the first-effect separator liquid inlet is communicated with the first-effect evaporator second liquid outlet;

The first-effect circulating pump includes an inlet of the first-effect circulating pump, a first outlet of the first-effect circulating pump, and a second outlet of the first-effect circulating pump. The first liquid outlet of the first-effect evaporator and the liquid outlet of the first-effect separator are both connected to The inlet of the first-effect circulating pump is communicated, and the first outlet of the first-effect circulating pump is communicated with the second liquid inlet of the first-effect evaporator;

The second evaporation and concentration device includes a second-effect evaporator, a second-effect separator, a second-effect circulating pump and a second-effect clear liquid tank;

The two-effect evaporator includes the first liquid inlet of the second-effect evaporator, the first vapor inlet of the second-effect evaporator, the second liquid inlet of the second-effect evaporator at the top, the first liquid outlet of the second-effect evaporator at the bottom, and the second-effect evaporator at the bottom. The second liquid outlet of the second effect evaporator and the second effect clear liquid outlet, the first liquid inlet of the second effect evaporator is communicated with the second outlet of the first effect circulating pump, and the first steam inlet of the second effect evaporator is connected to the The steam outlet of the first-effect separator is connected;

The second-effect separator includes a second-effect separator liquid inlet, a second-effect separator liquid outlet and a second-effect separator vapor outlet, and the second-effect separator liquid inlet is communicated with the second-effect evaporator second liquid outlet;

The two-effect circulating pump includes an inlet of the two-effect circulating pump, a first outlet of the two-effect circulating pump, and a second outlet of the two-effect circulating pump. The first liquid outlet of the two-effect evaporator and the liquid outlet of the two-effect separator are both connected to The inlet of the second-effect circulating pump is communicated with, and the first outlet of the second-effect circulating pump is communicated with the second liquid inlet of the second-effect evaporator;

The two-effect clear liquid tank includes an entrance of the two-effect clear liquid tank and an outlet of the two-effect clear liquid tank, and the entrance of the two-effect clear liquid tank is communicated with the two-effect clear liquid outlet;

The third evaporation and concentration device includes a three-effect evaporator, a three-effect separator and a three-effect circulating pump;

The triple-effect evaporator includes a first liquid inlet of the triple-effect evaporator, a first vapor inlet of the triple-effect evaporator, a second liquid inlet of the triple-effect evaporator, a liquid outlet of the triple-effect evaporator and an evaporative concentrated liquid outlet. The second liquid inlet of the evaporator is communicated with the second outlet of the two-effect circulating pump, the first liquid inlet of the three-effect evaporator is communicated with the outlet of the second-effect clear liquid tank, and the first steam inlet of the three-effect evaporator is communicated with the outlet of the second-effect clear liquid tank. The vapor outlet of the two-effect separator is communicated, and the evaporative concentrate outlet is communicated with the evaporative concentrate storage tank;

The three-effect separator includes the liquid inlet of the three-effect separator, the liquid outlet of the three-effect separator, the evaporative clear liquid outlet and the vapor outlet of the three-effect separator, the liquid inlet of the three-effect separator and the liquid outlet of the three-effect evaporator. be communicated, and the evaporative clear liquid outlet is communicated with the evaporative clear liquid storage tank;

The three-effect circulating pump comprises an outlet of the three-effect circulating pump, a first inlet of the three-effect circulating pump, and a second inlet of the three-effect circulating pump, and the outlet of the three-effect circulating pump 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 includes a terminal condenser inlet, a cooling water inlet, a first liquid outlet of the terminal condenser and a second liquid outlet of the terminal condenser, and the terminal condenser inlet is communicated with the steam outlet of the three-effect separator, so The first liquid outlet of the terminal condenser is communicated with the evaporative clear liquid storage tank, the second liquid outlet of the terminal condenser is communicated with the inlet of the terminal separator, and the vacuum pump is communicated with the outlet of the terminal separator .

Further, the rectification and dehydration system includes a primary rectification device or a multiple rectification device.

Further, the rectification dehydration system includes: a crude distillation column, a first rectification column, a second rectification column and an adsorber;

The crude distillation tower comprises an evaporative clear liquid inlet, an ethanol vapor outlet and a crude distillation tower clear liquid outlet, and the evaporative clear liquid inlet is communicated with the vaporized clear liquid storage tank;

The first rectifying tower comprises an ethanol vapor inlet, a fusel alcohol-containing light wine inlet and an ethanol clear liquid outlet, and the ethanol vapor inlet is communicated with the ethanol vapor outlet of the crude distillation tower;

The second rectification tower includes a rectification clear liquid inlet, a fusel alcohol-containing light wine outlet, an ethanol-containing clear liquid inlet and a semi-finished ethanol outlet, and the rectified clear liquid inlet is communicated with the crude distillation tower clear liquid outlet. , the outlet of the fusel alcohol-containing light wine is communicated with the inlet of the first rectification tower containing fusel alcohols; ;

The adsorber comprises an adsorber inlet and an adsorber outlet, the adsorber inlet is communicated with the semi-finished ethanol outlet, and the adsorber outlet is used for outputting ethanol products.

Further, the spray drying system includes a spray drying tower, the spray drying tower includes 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 The tower outlet is used to output protein powder.

One or more technical solutions in the embodiments of the present invention have at least the following technical effects or advantages:

The invention provides a method and system for co-producing protein powder by evaporation, concentration and rectification of fermented mash. The obtained evaporative concentrate is directly spray-dried to obtain protein powder, and the obtained evaporative clear liquid and membrane filtration clear liquid are jointly rectified The ethanol product is obtained by dehydration, the yield of the protein powder is high, the recovery rate of the ethanol product is not affected, the equipment system is not blocked, and the difficulty of protein sewage treatment is greatly reduced.

Description of drawings

In order to illustrate the technical solutions in the embodiments of the present invention more clearly, the following briefly introduces the accompanying drawings used in the description of the embodiments. Obviously, the drawings in the following description are some embodiments of the present invention. For those of ordinary skill in the art, other drawings can also be obtained from these drawings without any creative effort.

Fig. 1 is the flow chart of the method for a kind of fermented mash evaporation concentration and rectification co-production protein powder provided by the embodiment of the present invention;

2 is a structural diagram of a system for co-producing protein powder by evaporation and concentration of fermented mash and rectification provided by the embodiment of the present invention;

1. Evaporation and concentration system; 11. Evaporation and concentration device;

111, the first evaporation and concentration device; 1111, the first effect preheater; 1112, the first effect evaporator; 1A, the first liquid inlet of the first effect evaporator; 1B, the first vapor inlet of the first effect evaporator; 1C, the first effect evaporation 1D, first liquid outlet of first effect evaporator; 1E, second liquid outlet of first effect evaporator; 1113, first effect separation; 1F, first effect separator liquid inlet; 1G, first effect separator liquid outlet; 1H, the steam outlet of the first-effect separator; 1114, the first-effect circulating pump; 1I, the inlet of the first-effect circulating pump; 1J, the first outlet of the first-effect circulating pump; 1K, the second outlet of the first-effect circulating pump;

112, the second evaporation and concentration device; 1121, the second effect evaporator; 2A, the first liquid inlet of the second effect evaporator; 2B, the first vapor inlet of the second effect evaporator; 2C, the second liquid inlet of the second effect evaporator; 2D, The first liquid outlet of the second-effect evaporator; 2E, the second liquid outlet of the second-effect evaporator; 2F, the second-effect clear liquid outlet; 1122, the second-effect separator; 2G, the liquid inlet of the second-effect separator; 2H, the second-effect separator Liquid outlet; 2I, steam outlet of two-effect separator; 1123, two-effect circulating pump; 2J, two-effect circulating pump inlet; 2K, first outlet of two-effect circulating pump; 2L, second outlet of two-effect circulating pump; 1124, two-effect circulating pump clear liquid tank;

113, the third evaporation and concentration device; 1131, three-effect evaporator; 3A, the first liquid inlet of the three-effect evaporator; 3B, the first vapor inlet of the three-effect evaporator; 3C, the second liquid inlet of the three-effect evaporator; 3D, Three-effect evaporator liquid outlet; 3E, evaporation concentrate outlet; 1132, three-effect separator; 3F, three-effect separator liquid inlet; 3G, three-effect separator liquid outlet; 3H, evaporation clear liquid outlet; 3I, three-effect Separator steam outlet; 1133, three-effect circulating pump; 3J, three-effect circulating pump outlet; 3K, three-effect circulating pump first inlet; 3L, three-effect circulating pump second inlet;

114, terminal condenser; 4A, terminal condenser inlet; 4B, cooling water inlet; 4C, first liquid outlet of terminal condenser; 4D, second liquid outlet of terminal condenser; 115, terminal separator; 116, vacuum pump;

12. Evaporative concentrate storage tank;

13. Evaporated clear liquid storage tank;

2. Spray drying system; 21. Spray drying tower 21; 21A, spray drying tower inlet 2; 21B, spray drying tower outlet;

3. Rectification and dehydration system; 31. Crude distillation tower; 5A, clear liquid inlet; 5B, ethanol vapor outlet; 5C, crude distillation tower clear liquid outlet; 32, first rectification tower; 5D, ethanol vapor inlet; 5E , fusel alcohol-containing light wine inlet; 5F, ethanol-containing clear liquid outlet; 33, second rectification tower; 5G, rectification clear liquid inlet; 5H, fusel-containing light wine outlet; 5I, ethanol-containing clear liquid inlet ; 5J, semi-finished ethanol outlet; 34, adsorber; 5K, adsorber inlet; 5L, adsorber outlet.

Detailed ways

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 presented therefrom. It should be understood by those skilled in the art that these specific embodiments and examples are used to illustrate the present invention, but not to limit the present invention.

Throughout the specification, unless specifically stated otherwise, terms used herein are to be understood as commonly used in the art. Therefore, unless otherwise defined, 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. In case of conflict, the present specification takes precedence.

Unless otherwise specified, various raw materials, reagents, instruments and systems, etc. used in the present invention can be purchased from the market or can be prepared by existing methods.

The technical solutions provided by the embodiments of the present invention are as follows for solving the above-mentioned technical problems:

On the one hand, an embodiment of the present invention provides a method for co-producing protein powder by evaporation, concentration and rectification of fermented mash, as shown in Figure 1, comprising the following steps:

S1, obtain fermentation mature mash, described fermentation mature mash is carried out membrane filtration, obtain fermentation mash and membrane filtration clear liquid;

S2, the fermented mash is evaporated and concentrated to obtain evaporated concentrate and evaporated clear liquid;

S3, the evaporative concentrate is spray-dried to obtain protein powder;

S4, carrying out rectification and dehydration on the evaporation clear liquid and the membrane filtration clear liquid to obtain anhydrous ethanol product.

As can be seen from the above, in the present invention, the obtained evaporative concentrate is directly spray-dried to obtain protein powder, and the obtained evaporative clear liquid and membrane filtration clear liquid are jointly rectified and dehydrated to obtain an ethanol product. The yield of the protein powder is high, and the ethanol product is high. The water content is less than 0.8%, and the equipment system will not be blocked, and the difficulty of protein sewage treatment is greatly reduced.

In the prior art, the concentrated liquid and the clear liquid are usually passed through the rectification system together, and then the protein content in the concentrated liquid will block the equipment due to denaturation, etc., which will have an impact on the rectification system, and the recovery rate of centrifugal separation is low, causing A large amount of protein powder is lost, the yield of protein powder is very low, and the final output clear liquid contains bacterial protein, which has an impact on water treatment.

Preferably, the conditions for the evaporation and concentration are as follows: the concentration temperature is controlled at 45°C to 65°C, and the concentration of solids after concentration is 10% to 30%. Reduce the evaporative concentration temperature to reduce the chance of protein denaturation.

Preferably, the conditions of the spray drying are as follows: During spray drying, the inlet temperature of the hot air is 150°C to 210°C, the outlet temperature is 65°C to 85°C, and the temperature of the feed liquid is 35°C to 60°C. While ensuring protein water content, it will not affect the quality of protein powder products. Preferably, the conditions for the rectification and dehydration are as follows: the temperature of the crude tower tower reactor is less than 85°C, and the water content of the product ethanol is less than 0.8%. To ensure that the rectification system has sufficient thermocouples and performance, almost most of the ethanol is recovered, and the water content of the product meets the national standard. On the other hand, an embodiment of the present invention also provides a system for co-producing protein powder by evaporation and concentration of fermented mash and rectification as shown in Figure 2, including: an evaporation concentration system 1, a spray drying system 2 and a rectification dehydration system 3 ;

The evaporative concentration system 1 is used for evaporating and concentrating the fermented mash to obtain an evaporating concentrate and an evaporating clear liquid, including an evaporating and concentrating device 11, an evaporating and concentrating liquid storage tank 12 and an evaporating clear liquid storage tank 13. Both the liquid storage tank 12 and the evaporative clear liquid storage tank 13 are communicated with the evaporative concentration device 11;

The spray drying system 2 is communicated with the evaporative concentrate storage tank 12 for spray drying the evaporative concentrate;

The rectification and dehydration system 3 is communicated with the evaporative clear liquid storage tank 13, and is used for rectifying and dehydrating the membrane filtration clear liquid and the evaporative clear liquid to obtain an ethanol product.

The embodiment of the present invention provides a system for co-producing protein powder by evaporation, concentration and rectification of fermented mash. The storage tank 13 is connected, and the obtained evaporative concentrate is directly spray-dried to obtain protein powder, and the obtained evaporative clear liquid and membrane filtration clear liquid are jointly rectified and dehydrated to obtain an ethanol product. The yield of the protein powder is high, and the ethanol product is high. The water content is less than 0.8%, and the equipment system will not be blocked, and the difficulty of protein sewage treatment is greatly reduced.

The evaporative clear liquid storage tank 13 is provided with a membrane filtration clear liquid inlet, which is used to jointly transport the evaporative clear liquid and the membrane filtration clear liquid to the rectification dehydration system 2 rectification and dehydration to obtain ethanol products

Preferably, the evaporation and concentration device 11 includes a single-effect evaporation device or a multi-effect evaporation device.

Preferably, the evaporative concentration device 11 includes: a first evaporative concentration device 111, a second evaporative concentration device 112 and a third evaporative concentration device 113, a terminal condenser 114, a terminal separator 115 and a vacuum pump 116;

The first evaporation and concentration device 111 includes a first-effect preheater 1111, a first-effect evaporator 1112, a first-effect separator 1113 and a first-effect circulating pump 1114;

The first-effect preheater 1111 is used to heat the fermentation mash to obtain preheated fermentation mash;

The first-effect evaporator 1112 includes a first-effect evaporator first liquid inlet 1A, a first-effect evaporator first vapor inlet 1B, a first-effect evaporator second liquid inlet 1C at the top, and a first-effect evaporator first at the bottom. The liquid outlet 1D and the second liquid outlet 1E of the first-effect evaporator, the first liquid inlet 1A of the first-effect evaporator is communicated with the outlet of the first-effect preheater 1111, and the first vapor of the first-effect evaporator enters 1B The port is used to pass steam as a heat source;

The first-effect separator 1113 includes a first-effect separator liquid inlet 1F, a first-effect separator liquid outlet 1G and a first-effect separator vapor outlet 1H, the first-effect separator liquid inlet 1F and the first-effect evaporator second The liquid outlet is connected to 1E;

The first-effect circulating pump 1114 includes a first-effect circulating pump inlet 1I, a first-effect circulating pump first outlet 1J, a first-effect circulating pump second outlet 1K, the first-effect evaporator first liquid outlet 1D and the first-effect separation The liquid outlet 1G of the evaporator is all communicated with the inlet 1I of the first-effect circulating pump, and the first outlet 1J of the first-effect circulating pump is communicated with the second liquid inlet 1C of the first-effect evaporator;

The second evaporation and concentration device 112 includes 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 includes a first liquid inlet 2A of the second-effect evaporator, a first vapor inlet 2B of the second-effect evaporator, a second liquid inlet 2C of the second-effect evaporator at the top, and a second-effect evaporator at the bottom. The liquid outlet 2D, the second liquid outlet 2E of the second effect evaporator and the second effect clear liquid outlet 2F, the first liquid inlet 2A of the second effect evaporator is communicated with the second outlet 1K of the first effect circulating pump, and the second effect The first vapor inlet 2B of the evaporator is communicated with the vapor outlet 1H of the first-effect separator;

The second-effect separator 1122 includes a second-effect separator liquid inlet 2G, a second-effect separator liquid outlet 2H and a second-effect separator vapor outlet 2I, and the second-effect separator liquid inlet 2G is connected to the second-effect evaporator second. The liquid outlet is connected to 2E;

The second-effect circulating pump 1123 includes the second-effect circulating pump inlet 2J, the second-effect circulating pump first outlet 2K, the second-effect circulating pump second outlet 2L, the second-effect evaporator first liquid outlet 2D and the second-effect separation. The liquid outlet 2H of the evaporator is all communicated with the inlet 2J of the second-effect circulating pump, and the first outlet 2K of the second-effect circulating pump is communicated with the second liquid inlet 2C of the second-effect evaporator;

The two-effect clear liquid tank 1124 includes a two-effect clear liquid tank inlet and a two-effect clear liquid tank outlet, the two-effect clear liquid tank inlet is communicated with the two-effect clear liquid outlet 2F, and the two-effect clear liquid tank The outlet is communicated with the first liquid inlet of the triple-effect evaporator;

The third evaporation and concentration device 113 includes a three-effect evaporator 1131, a three-effect separator 1132 and a three-effect circulating pump 1133;

The triple-effect evaporator 1131 includes a first liquid inlet 3A of the triple-effect evaporator, a first vapor inlet 3B of the triple-effect evaporator, a second liquid inlet 3C of the triple-effect evaporator, a liquid outlet 3D of the triple-effect evaporator, and an evaporative concentrate outlet. 3E, the second liquid inlet 3C of the three-effect evaporator is communicated with the second outlet 2L of the second-effect circulating pump, and the first liquid inlet 3A of the triple-effect evaporator is communicated with the second-effect clear liquid tank outlet 2N, so The first steam inlet 3B of the three-effect evaporator is communicated with the steam outlet 2I of the second-effect separator, and the evaporative concentrate outlet 3E is communicated with the evaporative concentrate storage tank 12;

The three-effect separator 1132 includes the three-effect separator liquid inlet 3F, the three-effect separator liquid outlet 3G, the evaporation clear liquid outlet 3H and the three-effect separator vapor outlet 3I, the three-effect separator liquid inlet 3F and the three-effect separator liquid inlet 3F. The three-effect evaporator liquid outlet 3D is communicated with, and the evaporative clear liquid outlet 3H is communicated with the evaporative clear liquid storage tank;

The three-effect circulating pump 1133 includes an outlet 3J of the three-effect circulating pump, a first inlet 3K of the three-effect circulating pump, and a second inlet 3L of the three-effect circulating pump. The liquid inlet 3A is connected; the first inlet 3K of the three-effect circulating pump is connected with the second outlet 2L of the two-effect circulating pump, and the second inlet 3L of the three-effect circulating pump is connected with the liquid outlet 3G of the three-effect separator connected;

The terminal condenser 114 includes 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, and the terminal condenser inlet 4A is connected to the three-effect separator. The steam outlet 3I is communicated with, the first liquid outlet 4C of the terminal condenser is communicated with the evaporative clear liquid storage tank 13, and the second liquid outlet 4D of the terminal condenser is communicated with the inlet of the terminal separator 115, so The vacuum pump 116 communicates with the outlet of the terminal separator 115 .

It can be seen from the above that the fermented mash liquid first enters the first-effect preheater 1111 for preheating to obtain preheated fermented mash, enters the first-effect evaporator 1112 from the 1A port, and enters the first-effect evaporator 1112 from the 1B port with 6-8brag saturated steam as a heat source. ,

Port 2J of the first-effect circulating pump 1114 is communicated with port 1D of the first-effect evaporator and port 2H of the first-effect separator, and port 2K of the first-effect circulating pump is communicated with port 2C at the top of the first-effect evaporator, so that the inside of the first-effect evaporator is concentrated The liquid is circulated and heated, and the fermentation mash is initially concentrated by the first-effect evaporator 1112; the first-effect evaporator 1112 and the first-effect separator 1113 are communicated, and the first-effect separator 1113 is separated to obtain a first-effect evaporation concentrate;

The first-effect evaporation concentrate is transported to the second-effect evaporator 1121 by the first-effect circulating pump 1114 to be concentrated again; the first-effect separator 1113 conducts gas-liquid separation, and the generated steam is used as the heat source of the second-effect evaporator 1121; the second-effect circulation The inlet of the pump 1123 is communicated with the bottom of the second-effect evaporator 1121 and the second-effect separator 1122, the port 2K of the second-effect circulating pump is communicated with the port 2C at the top of the second-effect evaporator 1121, and circulates to heat and concentrate the evaporated concentrate; The effect separator 1122 is connected, and the separation is carried out in the second effect separator 1122 to obtain the second effect evaporation concentrate;

The outlet of the second-effect circulating pump 1123 is communicated with the third-effect circulating pump 1133, and the second-effect evaporation concentrate is sent to the third-effect evaporator 1131 for three-time concentration. Port 2I of the second-effect separator is connected with port 3B of the third-effect evaporator 1131, and serves as the heat source of the third-effect evaporator 1131; another part of the heat source;

The outlet of the three-effect circulating pump 1133 is connected with the bottom of the three-effect evaporator 1131, and the evaporated concentrate is circulated, heated and concentrated; the three-effect evaporator 1131 is connected with the three-effect separator 1132; the evaporated clear liquid and the evaporated clear liquid produced by the three-effect evaporator 1131 The storage tank 13 is connected, and the supernatant that almost does not contain bacterial protein is delivered;

The 3H port of the three-effect separator is communicated with the evaporative concentrate storage tank 12, and the evaporative concentrate with a concentration of 10%-30% and an ethanol content of less than 1 g/L is delivered;

The gas phase outlet of the three-effect separator 1132 is communicated with the terminal condenser 114, and the terminal condenser 114 is also connected with the evaporative clear liquid storage tank 13 to deliver clear liquid containing almost no bacterial protein; the evaporative clear liquid storage tank 13 also receives from Fermentation of the membrane filtered supernatant. The evaporating clear liquid storage tank 13 is communicated with the crude distillation tower 31 through a pump, and preliminarily separates the crude alcohol and water in the evaporating clear liquid.

The terminal condenser 114 is also communicated with the terminal separator 115, and the terminal separator 115 is communicated with the vacuum pump (16) to provide a negative pressure environment for the entire evaporation and concentration system;

Preferably, the rectification and dehydration system 3 includes a primary rectification device or a multiple rectification device.

Preferably, the rectification and dehydration system 3 includes: a crude distillation column 31, a first rectification column 32, a second rectification column 33 and an adsorber 34;

Described crude distillation tower 31 comprises evaporation clear liquid inlet 5A, ethanol vapor outlet 5B and crude distillation clear liquid outlet 5C, and described evaporated clear liquid inlet 5A communicates with described evaporated clear liquid storage tank 13;

The first rectifying tower 32 comprises an ethanol vapor inlet 5D, a fusel alcohol-containing light wine inlet 5E and an ethanol clear liquid outlet 5F, and the ethanol vapor inlet 5D is communicated with the crude distillation column ethanol vapor outlet 5B;

The second rectifying tower 33 includes a rectification clear liquid inlet 5G, a fusel alcohol-containing light wine outlet 5H, an ethanol clear liquid inlet 5I and a semi-finished ethanol outlet 5J, and the rectified clear liquid inlet 5G and the crude distillate The tower clear liquid outlet 5C communicates with each other, and the described fusel alcohol-containing light wine outlet 5H communicates with the first rectification tower fusel alcohol-containing light wine inlet 5E; the ethanol clear liquid inlet 5I is connected with the first The 5F outlet of the ethanol clear liquid of the rectification tower is connected;

The adsorber 34 includes an adsorber inlet 5K and an adsorber outlet 5L, the adsorber inlet 5K communicates with the semi-finished ethanol outlet 5J, and the adsorber outlet 5L is used for outputting ethanol products.

As can be seen from the above, the first rectifying column 32 is communicated with the top outlet 5B of the crude distillation column 31, and the first rectifying column 32 is also communicated with the upper part of the second rectifying column 33, receiving a part of the second rectifying column 33 containing fusel alcohols. Light wine; a part of the ethanol clear liquid in the crude distillation column 31 is transported to the second rectification column 33; about 95% concentration ethanol is extracted from the side of the first rectification column 32, and transported to the upper part of the second rectification column 33, the second rectification column The top of the distillation tower 33 outputs semi-finished ethanol with an ethanol concentration of ≥95% to the adsorber 34; the semi-finished ethanol removes most of the water through the adsorber 34, and the final product is an anhydrous ethanol product with a water content of less than 0.8%.

Preferably, the spray drying system 2 includes a spray drying tower 21, an air delivery system, a material receiving system and a packaging system, the spray drying tower 21 includes a spray drying tower inlet 21A and a spray drying tower outlet 21B, the spray drying tower The inlet 21A is communicated with the evaporative concentrate storage tank 12, and the outlet 21B of the spray drying tower is used for outputting protein powder. The air supply system, the material receiving system and the packaging system are not shown in the drawings, and the settings commonly used in the prior art can be used.

Preferably, the system for co-producing protein powder by evaporation, concentration and rectification of fermented mash may further include a membrane filtration system, and the membrane filtration system is used to perform membrane filtration on the fermented mash to obtain fermented mash and Membrane filtration of the supernatant.

A method and system for co-producing protein powder by evaporation, concentration and rectification of fermented mash according to the present application will be described in detail below in conjunction with the examples, comparative examples and experimental data.

Example 1

S1, obtain fermentation mash and membrane filtration clear liquid;

S2, the fermented mash is passed into the evaporative concentration system 1, for the fermented mash to be evaporated and concentrated, the evaporative concentrate and the evaporative clear liquid are obtained, the obtained evaporative concentrate is passed into the evaporative concentrate storage tank 12, and the obtained evaporation The clear liquid is passed into the evaporation clear liquid storage tank 13; the conditions for the evaporation and concentration are that the evaporation and concentration system adopts 0.6-0.8mpa saturated steam, adopts the three-effect evaporation falling film forced circulation evaporation type, and controls the evaporation and concentration system temperature ≤ 65 ℃, the evaporator concentrates Liquid ethanol content <0.08%.

S3. The evaporative concentrate storage tank 12 is communicated with the spray drying system 2, and is used to spray dry the evaporative concentrate to obtain protein powder; the conditions for spray drying are: the heat source of the spray drying tower is saturated with 0.6-0.8mpa Steam, using centrifugal spray drying type, control the inlet air temperature <180 ℃, the drying tower exhaust temperature 65-85 ℃.

S4, described evaporative clear liquid storage tank 13 is communicated with described rectification dehydration system 3, is used to carry out rectification dehydration with membrane filtration clear liquid and described evaporative clear liquid, obtains ethanol product; The condition of rectification dehydration is: The rectification heat source adopts 0.6-0.8mpa saturated steam, adopts three-column and molecular sieve dehydration system thermocouples and settings, and controls the bottom temperature of the crude distillation column in the control system < 85 ℃, and the water content of the product ethanol < 0.8%.

Example 2

S1, obtain fermentation mash and membrane filtration clear liquid;

S2, the fermented mash is passed into the evaporative concentration system 1, for the fermented mash to be evaporated and concentrated, the evaporative concentrate and the evaporative clear liquid are obtained, the obtained evaporative concentrate is passed into the evaporative concentrate storage tank 12, and the obtained evaporation The clear liquid is passed into the evaporation clear liquid storage tank 13; the conditions for evaporation and concentration are that the heat source of the evaporation and concentration system adopts hot water flash steam with a temperature of 120-150 °C, and multiple falling film forced circulation evaporators are set to control the temperature of the evaporation and concentration system to be ≤55 °C, The ethanol content of the evaporator concentrate is less than 0.08%. ...

S3, the evaporative concentrate storage tank 12 is communicated with the spray drying system 2, and is used for spray-drying the evaporative concentrate to obtain protein powder; the conditions for spray drying are: the heat source adopts a burner with CO as a raw material, The exhaust temperature of the burner is controlled at 150-210°C, and the pressure-type spray drying type is adopted.

S4, described evaporative clear liquid storage tank 13 is communicated with described rectification dehydration system 3, is used to carry out rectification dehydration with membrane filtration clear liquid and described evaporative clear liquid, obtains ethanol product; The condition of rectification dehydration is: Using 0.6-0.8mpa saturated steam as the heat source, set up a rectification tower and a crude distillation tower, and the rectification tower extracts 95% semi-finished ethanol into the dehydrator, and the final product is water <0.8% anhydrous ethanol. ...

Example 3

S1, obtain fermentation mash and membrane filtration clear liquid;

S2, the fermented mash is passed into the evaporative concentration system 1, for the fermented mash to be evaporated and concentrated, the evaporative concentrate and the evaporative clear liquid are obtained, the obtained evaporative concentrate is passed into the evaporative concentrate storage tank 12, and the obtained evaporation The clear liquid is passed into the evaporative clear liquid storage tank 13; the conditions for evaporative concentration are that the saturated steam is used as the heat source, the four-effect falling film forced circulation evaporation type is adopted, the temperature of the evaporator is controlled to be less than 65 degrees Celsius, and the ethanol content of the evaporated concentrate is less than 0.08%. The concentration of the concentrate is 30-35%.

S3. The evaporative concentrate storage tank 12 is communicated with the spray drying system 2, and is used to spray dry the evaporative concentrate to obtain protein powder; the conditions for spray drying are: using a heat source of 0.6-0.8mpa saturated steam Roller scraper dryer, control product moisture content <12%.

S4, described evaporative clear liquid storage tank 13 is communicated with described rectification dehydration system 3, is used to carry out rectification dehydration with membrane filtration clear liquid and described evaporative clear liquid, obtains ethanol product; The condition of rectification dehydration is: The rectification heat source adopts 0.6-0.8mpa saturated steam, adopts three-column rectification, pervaporation membrane dehydration, controls the bottom temperature of crude distillation column in the control system <85℃, pervaporation membrane operating pressure≤-0,9mpa, product ethanol water content <0.8%.

Comparative Example 1

In this comparative example, the concentrated liquid and the clear liquid go through the rectification system together.

S1, obtain fermentation mash and membrane filtration clear liquid;

S2. The fermented mash enters the crude distillation tower of the rectification system, the clear liquid filtered by the membrane enters the rectification tower 2# of the rectification system, and the 95% ethanol produced by the 2# rectification tower enters the molecular sieve dehydrator. The final product of the rectification and dehydration system is Water content <0.8% absolute ethanol;

S3. The residual distilled water of the crude distillation tower is separated by a centrifuge, and the centrifugal clear liquid is sent to the sewage treatment system

S4. The concentrate produced by the centrifuge is spray-dried, and the final product is protein powder.

Comparative Example 2

S1, obtain fermentation mash and membrane filtration clear liquid;

S2. The fermented mash enters the crude distillation tower of the rectification system, the clear liquid filtered by the membrane enters the second rectification tower of the rectification system, and the second rectification tower produces 95% ethanol into the molecular sieve dehydrator, and the final product of the rectification and dehydration system For water content <0.8% absolute ethanol;

S3. The residual distilled water of the crude distillation tower tower is concentrated by evaporation to obtain a 10%-30% evaporation concentrate, and the evaporated clear liquid is sent to sewage treatment

S4. The concentrate produced by the centrifuge is spray-dried, and the final product is protein powder.

Test Example 1

The yield of protein powder obtained in each embodiment and comparative example, the water content of the obtained ethanol product, the recovery rate of centrifugal separation in the rectification dehydration system, and the blockage of the rectification system are shown in Table 1.

Table 1

It can be seen from the data in Table 1 that:

In Comparative Example 1, the concentrated liquid and clear liquid are passed through the rectification system together, the yield of protein powder is only 70% to 80%, the recovery rate of centrifugal separation is low, the blockage of the rectification system is serious, and the cleaning frequency is high.

In Comparative Example 2, the conditions of evaporation and concentration are not within the scope of the present invention, and the cleaning cycle of the rectification system is long.

To sum up, the present invention provides a method and system for co-producing protein powder by evaporation, concentration and rectification of fermented mash. The ethanol product is obtained by jointly performing distillation and dehydration, the protein powder yield is high, the water content of the ethanol product is less than 0.8%, the equipment system will not be blocked, and the protein sewage treatment difficulty is greatly reduced.

Finally, it should also be noted that the terms "comprising", "comprising" or any other variation thereof are intended to encompass a non-exclusive inclusion such that a process, method, article or system comprising a series of elements includes not only those elements, but also Also included are other elements not expressly listed or inherent to such a process, method, article or system.

Although preferred embodiments of the present invention have been described, additional changes and modifications to these embodiments may occur to those skilled in the art once the basic inventive concepts are known. Therefore, the appended claims are intended to be construed to include the preferred embodiment and all changes and modifications that fall within the scope of the present invention.

It will be apparent to those skilled in the art that various modifications and variations can be made in the present invention without departing from the spirit and scope of the invention. Thus, provided that these modifications and variations of the present invention fall within the scope of the claims of the present invention and their equivalents, the present invention is also intended to include these modifications and variations.

Claims (10)

1. A method for co-producing albumen powder by evaporation concentration and rectification of fermented liquor is characterized by comprising the following steps:

obtaining fermented mash, and performing membrane filtration on the fermented mash to obtain fermented mash and membrane filtration clear liquid;

evaporating and concentrating the fermented mash to obtain an evaporated and concentrated solution and an evaporated clear solution;

spray drying the evaporated concentrated solution to obtain protein powder;

and rectifying and dehydrating the evaporated clear liquid and the membrane filtered clear liquid to obtain an absolute ethyl alcohol product.

2. The method for the evaporative concentration and rectification of protein powder produced from fermented mash according to claim 1, wherein the conditions of the evaporative concentration are as follows: the evaporation concentration temperature is controlled at 45-65 ℃, the concentration of the concentrated solid is 10-30%, and the ethanol content in the evaporation concentrated solution is less than 0.08%.

3. The method for the evaporative concentration and rectification of fermented mash to produce protein powder as claimed in claim 1, wherein the spray drying conditions are as follows: the hot air inlet temperature is 150-210 ℃, the outlet temperature is 65-85 ℃, and the feed liquid temperature is 35-80 ℃.

4. The method for the evaporative concentration and rectification of the protein powder produced by the fermentation mash according to claim 1, wherein the temperature of the bottom of the rough distillation tower is less than 85 ℃ during rectification dehydration, and the water content of the absolute ethyl alcohol product is less than 0.8%.

5. A system for co-producing albumen powder by evaporation concentration and rectification of fermented liquor is characterized by comprising: 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 rectifying and dehydrating the membrane filtration clear liquid and the evaporation clear liquid to obtain an absolute ethyl alcohol product.

6. The system for the evaporative concentration and rectification of protein powder produced from fermented mash according to claim 5, wherein the evaporative concentration device comprises a single-effect evaporation device or a multi-effect evaporation device.

7. The system for the evaporative concentration and rectification of protein powder produced by fermentation mash according to claim 5 or 6, 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.

8. The system for the evaporative concentration and rectification of fermented liquor and the co-production of protein powder according to claim 5, wherein the rectification dehydration system comprises a primary rectification device or a multi-rectification device.

9. The system for the evaporative concentration and rectification of protein powder produced by fermentation mash according to claim 5 or 8, wherein the rectification dehydration system comprises: the system comprises a rough 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.

10. The system for evaporative concentration and rectification of protein powder produced from fermented mash according to claim 5, 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.

Images