Liquefaction flash recovery system for trehalose production
The heat in the trehalose production process is recovered through the flash evaporation system and absorption system, which solves the problems of high energy consumption of the liquefied liquid heating and cooling, and achieves efficient energy utilization and cost reduction.
Patent Information
- Application Number
- CN202421590636.1
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-07-08
- Publication Date
- 2025-07-01
- Estimated Expiration
- 2034-07-08
AI Technical Summary
The heating and cooling of liquefied liquid during the trehalose production process requires a large amount of energy consumption, resulting in high energy consumption and increased production costs.
The flash evaporation system and absorption system are used to cool down through flash evaporation and absorb flash steam using low-temperature liquefied liquid to recover heat, combined with the jet-killing enzyme system to achieve cooling of high-temperature liquefied liquid and killing of amylase.
The reuse of heat is achieved, energy consumption is reduced, production costs are reduced, and energy utilization is improved.
Smart Images
Figure CN223042170U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to the technical field of trehalose production equipment, in particular to a liquefaction flash evaporation recovery system for trehalose production. Background Art
[0002] Trehalose is a non-reducing disaccharide formed by the combination of two glucose molecules through α,α-1,1 bonds. It widely exists in yeast, seaweed, molds, bacteria, insects and organisms. Through research, it is found that this sugar has unique biological functions, can protect biological macromolecules, cell membranes, and proteins from damage caused by freezing, drying, and osmotic pressure changes, and is widely used in the fields of food, medicine, cosmetics, health products, agriculture, etc.
[0003] At present, the main production methods of trehalose include microbial extraction method, fermentation method, enzyme conversion method, and genetic engineering method. Among them, the enzyme conversion method has broad application prospects due to its low cost, simple process, high conversion rate and other advantages. In the production of trehalose by the enzyme conversion method, starch is mainly used as the raw material. First, the starch is gelatinized, and then high-temperature amylase is added to catalyze the hydrolysis and liquefaction reaction of the gelatinized starch to obtain a liquefied starch solution. Then, the liquefied starch solution is sprayed for liquefaction to obtain a liquefied liquid. The temperature of the liquefied liquid is usually about 97°C. It is necessary to perform high-temperature enzyme inactivation treatment on the liquefied liquid to kill the high-temperature amylase in the liquefied liquid and avoid its influence on the subsequent saccharification process. The temperature of high-temperature enzyme inactivation is usually about 130°C. Then, after cooling the liquefied liquid to the saccharification temperature of about 60°C, trehalose synthase and trehalose hydrolase are added to the liquefied liquid to saccharify the liquefied liquid, and a saccharified crude liquid containing glucose, maltose, trehalose, trisaccharide and polysaccharide is obtained. The saccharified crude liquid is obtained after enzyme inactivation, protein removal and decolorization treatment. The saccharified clear liquid is passed through membrane separation and ion exchange to remove glucose, maltose, trisaccharide and polysaccharide in the saccharified clear liquid to obtain a trehalose solution. The trehalose solution is evaporated, concentrated and crystallized to obtain the finished trehalose.
[0004] As can be seen from the above, the temperature of the liquefied liquid is about 97°C, while the temperature of high-temperature enzyme inactivation is about 130°C. This requires heating and raising the temperature of the liquefied liquid, and the saccharification temperature is about 60°C. This requires cooling the liquefied liquid at about 130°C again. That is to say, in the liquefaction stage, the liquefied liquid needs to be heated and then cooled. Heating requires energy consumption, and cooling causes heat loss. This leads to high energy consumption and serious energy waste in the liquefaction stage. Moreover, cooling the liquefied liquid also requires a large amount of cooling water, which leads to high production cost and large energy consumption of trehalose. Summary of the Utility Model
[0005] In summary, in order to overcome the deficiencies of the prior art, the present utility model provides a liquefaction flash evaporation recovery system for trehalose production. It sends the high-temperature liquefied liquid at about 130 °C after enzyme inactivation into the flash evaporation system for flash evaporation and cooling. The low-temperature liquefied liquid at about 97 °C absorbs the flash evaporation steam, causing the low-temperature liquefied liquid to heat up, thereby realizing the recycling of the heat dissipated during the cooling process of the high-temperature liquefied liquid after enzyme inactivation, reducing energy consumption, improving energy utilization efficiency, and reducing production costs.
[0006] To solve the above technical problems, the technical solution adopted by the present utility model is as follows:
[0007] A liquefaction flash evaporation recovery system for trehalose production, which includes:
[0008] An injection enzyme inactivation system, the injection enzyme inactivation system has an injection pump, a steam injector and a pressure-bearing tank. The feed port of the injection pump is connected to the absorption system, the discharge port of the injection pump is connected to the feed port of the steam injector, the intake port of the steam injector is connected to the steam source through a steam pipeline, the discharge port of the steam injector is connected to the feed port of the pressure-bearing tank, and the discharge port of the pressure-bearing tank is connected to the flash evaporation system.
[0009] A flash evaporation system, the flash evaporation system has n flash tanks. The high-temperature liquefied liquid after enzyme inactivation flows through the first-stage flash tank, the second-stage flash tank, and until the nth-stage flash tank in sequence. The feed port of the first-stage flash tank is connected to the discharge port of the pressure-bearing tank, and the discharge port of the nth-stage flash tank is connected to the subsequent saccharification process.
[0010] An absorption system, the absorption system has m absorption towers. The m absorption towers have a total of n absorption units, where n is a positive integer multiple of m. The low-temperature liquefied liquid flows through the first-stage absorption unit, the second-stage absorption unit, and until the nth-stage absorption unit in sequence. The feed port of the first-stage absorption unit is connected to the liquefied liquid tank, and the discharge port of the nth-stage absorption unit is connected to the feed port of the injection pump.
[0011] The gas outlet of the nth-stage absorption unit is connected to the gas inlet of the n - 1th-stage absorption unit, the gas outlet of the n - 1th-stage absorption unit is connected to the gas inlet of the n - 2th-stage absorption unit, and so on. The gas inlet of the second-stage absorption unit is connected to the gas inlet of the first-stage absorption unit, and the gas outlet of the first-stage absorption unit is connected to the tail gas treatment system.
[0012] The flash evaporation gas outlet of the nth-stage flash tank is connected to the gas inlet of the first-stage absorption unit, the flash evaporation gas outlet of the n - 1th-stage flash tank is connected to the gas inlet of the second-stage absorption unit, and so on. The flash evaporation gas outlet of the first-stage flash tank is connected to the gas inlet of the nth-stage absorption unit.
[0013] Further, the absorption tower is a single-stage absorption tower, and one absorption tower is one absorption unit. The absorption system has m absorption towers, where m is equal to n. The low-temperature liquefied liquid before sterilization flows through the first-stage absorption tower, the second-stage absorption tower, and so on until the nth-stage absorption tower in sequence; or, the absorption tower is a combined absorption tower, and one absorption tower has a-stage absorption units. The absorption system has m absorption towers, where n = m * a, and a is a positive integer greater than or equal to 2; or, the absorption tower is a combination of a single-stage absorption tower and a combined absorption tower.
[0014] Further, the flash evaporation system has six flash tanks. The high-temperature liquefied liquid after enzyme inactivation flows through the first-stage flash tank, the second-stage flash tank, the third-stage flash tank, the fourth-stage flash tank, the fifth-stage flash tank, and the sixth-stage flash tank in sequence.
[0015] The absorption system has two absorption towers, namely the first absorption tower and the second absorption tower. Both the first absorption tower and the second absorption tower are vertical three-stage combined absorption towers. One absorption tower has three-stage absorption units. The first absorption tower has a first-stage absorption unit, a second-stage absorption unit, and a third-stage absorption unit that are connected in sequence from top to bottom. The second absorption tower has a fourth-stage absorption unit, a fifth-stage absorption unit, and a sixth-stage absorption unit that are connected in sequence from top to bottom.
[0016] The flash vapor outlet of the first-stage flash tank is connected to the air inlet of the sixth-stage absorption unit of the second absorption tower. The flash vapor outlet of the second-stage flash tank is connected to the air inlet of the fifth-stage absorption unit of the second absorption tower. The flash vapor outlet of the third-stage flash tank is connected to the air inlet of the fourth-stage absorption unit of the second absorption tower. The air outlet of the second absorption tower is connected to the air inlet of the third-stage absorption unit of the first absorption tower.
[0017] The flash vapor outlet of the fourth-stage flash tank is connected to the air inlet of the third-stage absorption unit of the first absorption tower. The flash vapor outlet of the fifth-stage flash tank is connected to the air inlet of the second-stage absorption unit of the first absorption tower. The flash vapor outlet of the sixth-stage flash tank is connected to the air inlet of the first-stage absorption unit of the first absorption tower.
[0018] Further, it also includes a transfer pump. Between adjacent two of the m absorption towers through which the liquefied liquid flows before enzyme inactivation, a transfer pump is provided. The feed inlet of the transfer pump is connected to the discharge outlet of the previous absorption tower among the adjacent two absorption towers, and the discharge outlet of the transfer pump is connected to the feed inlet of the subsequent absorption tower.
[0019] Further, the absorption tower has an absorption liquid level gauge. The absorption liquid level gauge on the absorption tower connected to the feed inlet of the transfer pump is electrically connected to the transfer pump. The motor frequency of the transfer pump is controlled and adjusted through the absorption liquid level gauge. The absorption liquid level gauge on the absorption tower connected to the feed inlet of the injection pump is electrically connected to the injection pump. The motor frequency of the injection pump is controlled through this absorption liquid level gauge.
[0020] Further, a steam inlet valve is provided on the steam pipeline where the inlet of the steam ejector is communicated with the steam source. A jet temperature sensor is provided on the pipeline where the outlet of the steam ejector is communicated with the inlet of the pressure-bearing tank. The jet temperature sensor is electrically connected to the steam inlet valve, and the steam inlet valve is controlled and adjusted through the jet temperature sensor.
[0021] Further, the pressure-bearing tank is equipped with a pressure-bearing tank pressure sensor. A flash feed valve is provided on the pipeline where the outlet of the pressure-bearing tank is communicated with the inlet of the first-stage flash tank. The pressure-bearing tank pressure sensor is electrically connected to the flash feed valve, and the flash feed valve is controlled and adjusted through the pressure-bearing tank pressure sensor.
[0022] Further, each of the n flash tanks of the flash system is equipped with a flash pressure sensor and a flash liquid level gauge. The outlet of the flash tank is equipped with a flash temperature sensor. Among them, the flash liquid level gauge of the nth-stage flash tank is electrically connected to the outlet valve. The outlet valve is provided on the pipeline where the outlet of the nth-stage flash tank is communicated with the subsequent saccharification process. The outlet valve is controlled and adjusted through the flash liquid level gauge of the nth-stage flash tank.
[0023] Further, the absorption tower where the first-stage absorption unit is located is equipped with a first-stage absorption pressure sensor. An exhaust valve is provided on the pipeline where the first-stage absorption unit is communicated with the tail gas treatment system. The first-stage absorption pressure sensor is electrically connected to the exhaust valve, and the exhaust valve is controlled and adjusted through the first-stage absorption pressure sensor.
[0024] The beneficial effects of the present utility model are as follows:
[0025] 1. The present utility model sends the high-temperature liquefied liquid at about 130 °C after enzyme inactivation into the flash system for flash cooling. The low-temperature liquefied liquid at about 97 °C absorbs the flash steam, so that the low-temperature liquefied liquid is heated up, thereby realizing the recovery and reuse of the heat dissipated during the cooling process of the high-temperature liquefied liquid at about 130 °C after enzyme inactivation, reducing energy consumption, improving energy utilization rate, and reducing production costs.
[0026] 2. The flash system of the present utility model can flash out flash steam while cooling the liquefied liquid after enzyme inactivation. The flash steam enters the absorption system, and the liquefied liquid absorbs the flash steam, and the temperature of the liquefied liquid rises. The flash system of the present utility model adopts six-stage flash tanks, which can perform six-stage flash cooling on the liquefied liquid at about 130 °C after enzyme inactivation, cooling the temperature to about 103 °C, and at the same time providing six flash steams at different temperatures for the absorption system. After the absorption system of the present utility model absorbs the six flash steams at different temperatures, it can heat the liquefied liquid at about 97 °C to about 123 °C. The flash steam generated during the flash cooling process is used to heat the liquefied liquid, realizing the recovery and reuse of heat, thereby reducing production costs.
[0027] 3. The jet enzyme inactivation system of the present utility model includes a jet pump, a steam injector and a pressure-bearing tank. The jet pump pressurizes the liquefied liquid flowing out of the absorption system and then transports it to the steam injector. Under the jet action of the live steam provided by the steam source, the high-speed jet steam carries the liquefied liquid and jets and flows. During the flowing process, the high-temperature live steam is absorbed by the liquefied liquid, and the live steam further heats the liquefied liquid, raising the temperature of the liquefied liquid to about 130 °C. Under the action of the high temperature, the amylase in the liquefied liquid is inactivated, achieving the enzyme inactivation effect.
[0028] 4. The present utility model has a simple structure, is convenient to use and has a low cost. It can effectively realize the recovery and reuse of waste heat in the production process of trehalose, effectively improve the energy utilization rate, reduce the production cost of trehalose, and enhance the market competitiveness of the enterprise. BRIEF DESCRIPTION OF THE DRAWINGS
[0029] Figure 1 It is a schematic structural diagram of the present utility model. DETAILED DESCRIPTION OF THE EMBODIMENTS
[0030] The present utility model will be further described in detail below with reference to the drawings.
[0031] Such as Figure 1As shown in the figure, a trehalose production liquefaction flash evaporation recovery system includes a jet enzyme inactivation system, an absorption system and a flash evaporation system. The absorption system has m absorption towers, and the m absorption towers have a total of n absorption units. n is a positive integer multiple of m. The low-temperature liquefied liquid before enzyme inactivation flows through the first-stage absorption unit 201, the second-stage absorption unit 202, and so on until the nth-stage absorption unit in sequence. The gas outlet of the nth-stage absorption unit is connected to the gas inlet of the (n - 1)th-stage absorption unit, and the gas outlet of the (n - 1)th-stage absorption unit is connected to the gas inlet of the (n - 2)th-stage absorption unit, and so on. The gas inlet of the second-stage absorption unit 202 is connected to the gas inlet of the first-stage absorption unit 201, and the gas outlet of the first-stage absorption unit 201 is connected to the tail gas treatment system. The feed port of the first-stage absorption unit 201 is connected to the liquefied liquid tank 1, and the discharge port of the nth-stage absorption unit is connected to the feed port of the jet enzyme inactivation system. The jet enzyme inactivation system has a jet pump 5, a steam injector 6 and a pressure-bearing tank 7. The feed port of the jet pump 5 is connected to the discharge port of the nth-stage absorption unit, the discharge port of the jet pump 5 is connected to the feed port of the steam injector 6, and the gas inlet of the steam injector 6 is connected to the steam source 14 through a steam pipeline 16. The discharge port of the steam injector 6 is connected to the feed port of the pressure-bearing tank 7. The discharge port of the pressure-bearing tank 7 is connected to the flash evaporation system. The flash evaporation system has n flash tanks. The high-temperature liquefied liquid after enzyme inactivation flows through the first-stage flash tank 8, the second-stage flash tank 9, and so on until the nth-stage flash tank in sequence. The feed port of the first-stage flash tank 8 is connected to the discharge port of the pressure-bearing tank 7, and the discharge port of the nth-stage flash tank is connected to the subsequent saccharification process. The flash vapor outlet of the nth-stage flash tank is connected to the gas inlet of the first-stage absorption unit 201, and the flash vapor outlet of the (n - 1)th-stage flash tank is connected to the gas inlet of the second-stage absorption unit 202, and so on. The flash vapor outlet of the first-stage flash tank 8 is connected to the gas inlet of the nth-stage absorption unit.
[0032] In this embodiment, the flash evaporation system has six flash evaporation tanks, namely the primary flash evaporation tank 8, the secondary flash evaporation tank 9, the tertiary flash evaporation tank 10, the quaternary flash evaporation tank 11, the quinary flash evaporation tank 12, and the senary flash evaporation tank 13 through which the enzyme-inactivated liquefied liquid flows in sequence. The feed inlet of the primary flash evaporation tank 8 is connected to the discharge outlet of the pressure-bearing tank 7, and the discharge outlet of the senary flash evaporation tank 13 is connected to the subsequent saccharification process. In this embodiment, the absorption system has two absorption towers, namely the first absorption tower 2 and the second absorption tower 4. Both the first absorption tower 2 and the second absorption tower 4 are vertical three-stage combined absorption towers. One absorption tower has three-stage absorption units 203. The first absorption tower 2 has a primary absorption unit 201, a secondary absorption unit 202, and a tertiary absorption unit 203 connected in sequence from top to bottom. The second absorption tower 4 has a quaternary absorption unit 401, a quinary absorption unit 402, and a senary absorption unit 403 connected in sequence from top to bottom. The feed inlet of the first absorption tower 2 is connected to the liquefied liquid tank 1. The discharge outlet of the first absorption tower 2 is connected to the feed inlet of the transfer pump 3. The discharge outlet of the transfer pump 3 is connected to the feed inlet of the second absorption tower 4. The discharge outlet of the second absorption tower 4 is connected to the feed inlet of the ejector pump 5. The flash vapor outlet of the primary flash evaporation tank 8 is connected to the gas inlet of the senary absorption unit 403 of the second absorption tower 4. The flash vapor outlet of the secondary flash evaporation tank 9 is connected to the gas inlet of the quinary absorption unit 402 of the second absorption tower 4. The flash vapor outlet of the tertiary flash evaporation tank 10 is connected to the gas inlet of the quaternary absorption unit 401 of the second absorption tower 4. The flash vapor outlet of the quaternary flash evaporation tank 11 is connected to the gas inlet of the tertiary absorption unit 203 of the first absorption tower 2. The gas outlet of the second absorption tower 4 is connected to the gas inlet of the tertiary absorption unit 203 of the first absorption tower 2. The flash vapor outlet of the quinary flash evaporation tank 12 is connected to the gas inlet of the secondary absorption unit 202 of the first absorption tower 2. The flash vapor outlet of the senary flash evaporation tank 13 is connected to the gas inlet of the primary absorption unit 201 of the first absorption tower 2. The gas outlet of the first absorption tower 2 is connected to the tail gas treatment system.
[0033] On the steam pipeline 16 where the gas inlet of the steam ejector 6 is connected to the steam source 14, a steam inlet valve 15 is provided. On the pipeline where the discharge outlet of the steam ejector 6 is connected to the feed inlet of the pressure-bearing tank 7, a jet temperature sensor 17 is provided. The jet temperature sensor 17 is electrically connected to the steam inlet valve 15, and the steam inlet valve 15 is controlled and adjusted by the jet temperature sensor 17. The pressure-bearing tank 7 is equipped with a pressure-bearing tank pressure sensor 19. On the pipeline where the discharge outlet of the pressure-bearing tank 7 is connected to the feed inlet of the primary flash evaporation tank 8, a flash evaporation feed valve 18 is provided. The pressure-bearing tank pressure sensor 19 is electrically connected to the flash evaporation feed valve 18, and the flash evaporation feed valve 18 is controlled and adjusted by the pressure-bearing tank pressure sensor 19.
[0034] Each of the six flash tanks in the flash evaporation system is equipped with a flash evaporation pressure sensor and a flash evaporation level gauge. The discharge port of the flash tank is equipped with a flash evaporation temperature sensor. Among them, the flash evaporation level gauge 21 of the sixth-stage flash tank 13 is electrically connected to the discharge valve 22. The discharge valve 22 is arranged on the pipeline connecting the discharge port of the sixth-stage flash tank 13 and the subsequent saccharification process. The discharge valve 22 is controlled and adjusted through the flash evaporation level gauge 21 of the sixth-stage flash tank 13.
[0035] The first absorption tower 2 connected to the inlet of the transfer pump 3 is equipped with a first absorption level gauge 23. The first absorption level gauge 23 is electrically connected to the transfer pump 3. The motor frequency of the transfer pump 3 is controlled and adjusted through the first absorption level gauge 23. The first absorption tower 2 is equipped with a first-stage absorption pressure sensor 24. An exhaust valve 25 is arranged on the pipeline connecting the gas outlet of the first absorption tower 2 and the tail gas treatment system. The first-stage absorption pressure sensor 24 is electrically connected to the exhaust valve 25. The exhaust valve 25 is controlled and adjusted through the first-stage absorption pressure sensor 24. The second absorption tower 4 is equipped with a second absorption level gauge 20. The second absorption level gauge 20 is electrically connected to the ejector pump 5. The motor frequency of the ejector pump 3 is controlled and adjusted through the second absorption level gauge 20.
[0036] During use, the temperature of the liquefied liquid stored in the liquefied liquid tank 1 is about 97 °C. Under the action of the transfer pump 3, the liquefied liquid in the liquefied liquid tank 1 enters from the top of the first absorption tower 2. In the first absorption tower 2, the liquefied liquid flows downward, successively passing through the first-stage absorption unit 201, the second-stage absorption unit 202, and the third-stage absorption unit 203 arranged from top to bottom in the first absorption tower 2, and flows out from the discharge port at the lower end of the first absorption tower 2. Under the action of the transfer pump 3, it enters from the top of the second absorption tower 4. In the second absorption tower 4, it flows downward, successively passing through the fourth-stage absorption unit 401, the fifth-stage absorption unit 402, and the sixth-stage absorption unit 403 arranged from top to bottom in the second absorption tower 4, and flows out from the discharge port at the lower end of the second absorption tower 4.
[0037] The temperature of the liquefied liquid after being sprayed by the steam ejector 6 is about 130 °C. The liquefied liquid at about 130 °C enters the flash evaporation system, successively passing through the six flash tanks in the flash evaporation system. The liquefied liquid after six times of flash evaporation and temperature reduction enters the subsequent saccharification process. The temperature of the liquefied liquid after six times of flash evaporation and temperature reduction is about 103 °C. During the flash evaporation process, the first flash tank 8 flashes out the first flash vapor, the second flash tank 9 flashes out the second flash vapor, and so on. The sixth flash tank 13 flashes out the sixth flash vapor. The temperature of the first flash vapor > the second flash vapor > the third flash vapor > the fourth flash vapor > the fifth flash vapor > the sixth flash vapor.
[0038] The temperature of the sixth flash vapor flashed out by the sixth flash tank 13 is the lowest. The sixth flash vapor enters the first-stage absorption unit 201 of the first absorption tower 2. In the first-stage absorption unit 201, the sixth flash vapor is absorbed by the liquefied liquid, and the liquefied liquid is heated for the first time.
[0039] The five - stage flash vapor flashed out from the five - stage flash tank 12 enters the secondary absorption unit 202 of the first absorption tower 2. Inside the secondary absorption unit 202, the five - stage flash vapor is absorbed by the liquefied liquid, and the liquefied liquid is heated for the second time.
[0040] The four - stage flash vapor flashed out from the four - stage flash tank 11 enters the tertiary absorption unit 203 of the first absorption tower 2. Inside the tertiary absorption unit 203, the four - stage flash vapor is absorbed by the liquefied liquid, and the liquefied liquid is heated for the third time. After being heated three times, the temperature of the liquefied liquid is about 110 °C. Then, under the action of the transfer pump 3, the liquefied liquid after being heated three times enters the second absorption tower 4.
[0041] The three - stage flash vapor flashed out from the three - stage flash tank 10 enters the quaternary absorption unit 401 of the second absorption tower 4. Inside the quaternary absorption unit 401, the three - stage flash vapor is absorbed by the liquefied liquid, and the liquefied liquid is heated for the fourth time.
[0042] The two - stage flash vapor flashed out from the two - stage flash tank 9 enters the quinary absorption unit 402 of the second absorption tower 4. Inside the quinary absorption unit 402, the two - stage flash vapor is absorbed by the liquefied liquid, and the liquefied liquid is heated for the fifth time.
[0043] The temperature of the primary flash vapor flashed out from the primary flash tank 8 is the highest. The primary flash vapor enters the senary absorption unit 403 of the second absorption tower 4. Inside the senary absorption unit 403, the primary flash vapor is absorbed by the liquefied liquid, and the liquefied liquid is heated for the sixth time. After being heated six times, the temperature of the liquefied liquid is about 123 °C. The liquefied liquid after being heated six times flows out from the discharge port at the lower end of the second absorption tower 4. Under the action of the ejector pump 5, the liquefied liquid is transported to the steam ejector 6. The live steam provided by the steam source 14 enters the steam ejector 6. Under the action of the steam ejector 6, the live steam carries the liquefied liquid and sprays it into the pressure - bearing tank 7 at a high speed. At this time, the temperature of the liquefied liquid is about 130 °C. Under the action of the high temperature, the amylase in the liquefied liquid is killed. The liquefied liquid at about 130 °C flowing out from the pressure - bearing tank 7 enters the flash system for flashing. In this way, by recycling the flash vapor flowing out from the flash system and using the flash vapor to heat the liquefied liquid, the consumption of live steam can be effectively reduced and energy can be saved.
[0044] It should be noted that the above - described embodiments are illustrative rather than restrictive of the technical solutions of the present invention. Equivalent substitutions by those of ordinary skill in the art or other modifications made according to the prior art, as long as they do not exceed the idea and scope of the technical solutions of the present invention, shall be included within the scope of the rights required by the present invention.
Claims
1. A trehalose production liquefaction flash recovery system, characterized in that: include: The jet enzyme inactivation system comprises a jet pump, a steam ejector and a pressure tank, wherein the feed port of the jet pump is connected to the absorption system, the discharge port of the jet pump is connected to the feed port of the steam ejector, the air inlet of the steam ejector is connected to the steam source through a steam pipeline, the discharge port of the steam ejector is connected to the feed port of the pressure tank, and the discharge port of the pressure tank is connected to the flash evaporation system. The flash evaporation system has n flash evaporation tanks. The high-temperature liquefied liquid after enzyme inactivation flows through the first-stage flash evaporation tank, the second-stage flash evaporation tank, and finally the n-stage flash evaporation tank in sequence. The feed port of the first-stage flash evaporation tank is connected to the discharge port of the pressure tank, and the discharge port of the n-stage flash evaporation tank is connected to the subsequent saccharification process. The absorption system comprises m absorption towers, the m absorption towers have n-stage absorption units, n is a positive integer multiple of m, the low-temperature liquefied liquid before enzyme inactivation flows sequentially through the primary absorption unit, the secondary absorption unit, and finally the n-stage absorption unit, the feed port of the primary absorption unit is connected to the liquefied liquid tank, and the discharge port of the n-stage absorption unit is connected to the feed port of the jet pump, The gas outlet of the n-stage absorption unit is connected to the gas inlet of the n-1-stage absorption unit, the gas outlet of the n-1-stage absorption unit is connected to the gas inlet of the n-2-stage absorption unit, and so on, the gas inlet of the secondary absorption unit is connected to the gas inlet of the primary absorption unit, and the gas outlet of the primary absorption unit is connected to the tail gas treatment system. The flash gas outlet of the n-stage flash tank is connected to the air inlet of the first-stage absorption unit, the flash gas outlet of the n-1-stage flash tank is connected to the air inlet of the second-stage absorption unit, and so on. The flash gas outlet of the first-stage flash tank is connected to the air inlet of the n-stage absorption unit.
2. The trehalose production liquefaction flash recovery system according to claim 1, characterized in that: The absorption tower is a single-stage absorption tower, one absorption tower is one absorption unit, and the absorption system has m absorption towers, where m is equal to n. The low-temperature liquefied liquid before sterilization flows through the first-stage absorption tower, the second-stage absorption tower, and finally the n-stage absorption tower in sequence; or, the absorption tower is a combined absorption tower, one absorption tower has an a-stage absorption unit, and the absorption system has m absorption towers, where n=m*a, and a is a positive integer greater than or equal to 2; or, the absorption tower is a combination of a single-stage absorption tower and a combined absorption tower.
3. The trehalose production liquefaction flash recovery system according to claim 2, characterized in that: The flash evaporation system has six flash evaporation tanks. The high-temperature liquefied liquid after enzyme inactivation flows through the first-stage flash evaporation tank, the second-stage flash evaporation tank, the third-stage flash evaporation tank, the fourth-stage flash evaporation tank, the fifth-stage flash evaporation tank and the sixth-stage flash evaporation tank in sequence. The absorption system has two absorption towers, namely the first absorption tower and the second absorption tower. Both the first absorption tower and the second absorption tower are vertical three-stage combined absorption towers. One absorption tower has three absorption units. The first absorption tower has a first absorption unit, a second absorption unit and a third absorption unit connected in sequence from top to bottom. The second absorption tower has a fourth absorption unit, a fifth absorption unit and a sixth absorption unit connected in sequence from top to bottom. The flash gas outlet of the first flash tank is connected to the air inlet of the sixth-stage absorption unit of the second absorption tower, the flash gas outlet of the second flash tank is connected to the air inlet of the fifth-stage absorption unit of the second absorption tower, the flash gas outlet of the third flash tank is connected to the air inlet of the fourth-stage absorption unit of the second absorption tower, and the gas outlet of the second absorption tower is connected to the air inlet of the third-stage absorption unit of the first absorption tower. The flash gas outlet of the fourth-stage flash tank is connected to the air inlet of the third-stage absorption unit of the first absorption tower, the flash gas outlet of the fifth-stage flash tank is connected to the air inlet of the second-stage absorption unit of the first absorption tower, and the flash gas outlet of the sixth-stage flash tank is connected to the air inlet of the first-stage absorption unit of the first absorption tower.
4. The trehalose production liquefaction flash recovery system according to any one of claims 1 to 3, characterized in that: It also includes a delivery pump. Among the m absorption towers through which the low-temperature liquefied liquid before enzyme inactivation flows in sequence, a delivery pump is arranged between two adjacent absorption towers. The feed port of the delivery pump is connected to the discharge port of the front absorption tower among the two adjacent absorption towers, and the discharge port of the delivery pump is connected to the feed port of the rear absorption tower.
5. The trehalose production liquefaction flash recovery system according to claim 4, characterized in that: The absorption tower is provided with an absorption level gauge. The absorption level gauge on the absorption tower connected to the feed port of the delivery pump is electrically connected to the delivery pump. The motor frequency of the delivery pump is controlled and adjusted by the absorption level gauge. The absorption level gauge on the absorption tower connected to the feed port of the jet pump is electrically connected to the jet pump. The motor frequency of the jet pump is controlled by the absorption level gauge.
6. The trehalose production liquefaction flash recovery system according to claim 1, characterized in that: A steam inlet valve is arranged on the steam pipeline connecting the air inlet of the steam ejector with the steam source, an injection temperature sensor is arranged on the pipeline connecting the discharge port of the steam ejector with the feed port of the pressure tank, the injection temperature sensor is electrically connected to the steam inlet valve, and the steam inlet valve is controlled and regulated by the injection temperature sensor.
7. The trehalose production liquefaction flash recovery system according to claim 6, characterized in that: The pressure tank has a pressure tank pressure sensor, a flash feed valve is arranged on the pipeline connecting the discharge port of the pressure tank and the feed port of the first-stage flash tank, the pressure tank pressure sensor is electrically connected to the flash feed valve, and the flash feed valve is controlled and regulated by the pressure tank pressure sensor.
8. The trehalose production liquefaction flash recovery system according to claim 1, characterized in that: The n flash tanks of the flash evaporation system are all provided with a flash evaporation pressure sensor and a flash evaporation level gauge, and the discharge port of the flash evaporation tank is provided with a flash evaporation temperature sensor, wherein the flash evaporation level gauge of the n-stage flash evaporation tank is electrically connected to the discharge valve, and the discharge valve is arranged on a pipeline connecting the discharge port of the n-stage flash evaporation tank and a subsequent saccharification process, and the discharge valve is controlled and regulated by the flash evaporation level gauge of the n-stage flash evaporation tank.
9. The trehalose production liquefaction flash recovery system according to claim 1, characterized in that: The absorption tower where the primary absorption unit is located has a primary absorption pressure sensor. An exhaust valve is arranged on the pipeline connecting the primary absorption unit and the tail gas treatment system. The primary absorption pressure sensor is electrically connected to the exhaust valve, and the exhaust valve is controlled and regulated by the primary absorption pressure sensor.