Rice syrup evaporation, concentration and cooling device

Abstract

The utility model discloses a rice syrup evaporation, concentration and cooling device which is characterized in that an outlet of a saccharification liquid buffer tank is connected with an inlet of a first-effect evaporator through a saccharification liquid delivery pump, an outlet of the first-effect evaporator is connected with an inlet of an auxiliary first-effect evaporator, and an outlet of the auxiliary first-effect evaporator is connected with an inlet of a second-effect evaporator; an outlet of the second-effect evaporator is connected with an inlet of the third-effect evaporator, and an outlet of the third-effect evaporator is connected with the vertical cooling crystallizer through the high-viscosity rotor pump; live steam serves as a first-effect heat source, gelatinization flash steam serves as an auxiliary first-effect heat source, secondary steam of a first-effect separator, secondary steam of an auxiliary first-effect separator and saccharification flash steam serve as heat sources of a second-effect evaporator, and secondary steam of the second-effect separator serves as a heat source of a third-effect evaporator; a secondary steam outlet of the triple-effect separator and each-effect non-condensable gas extraction opening are jointly connected with a shell pass inlet of a condenser; and a shell pass exhaust opening of the condenser is communicated with the atmosphere through a water-ring vacuum pump. The device is low in investment, small in occupied area, high in evaporation efficiency, good in syrup quality and low in production energy consumption.

Description

Technical Field

[0001] The utility model relates to an evaporation concentration device, in particular to a rice syrup evaporation concentration cooling device, belonging to the technical field of syrup concentration equipment. Background Art

[0002] In the process of rice processing, about 20% rice husks, 15% broken rice and 10% rice bran are produced as by-products. These by-products are rich in protein, fat, starch, etc. Normally, we use broken rice and rice bran as feed and rice husk as fuel, which not only wastes resources but also has a certain impact on the environment.

[0003] Broken rice contains high-quality starch and protein as a by-product. Broken rice starch can be processed into crystalline sugar through pulping, liquefaction, separation, saccharification and refining, evaporation and concentration, cooling and crystallization, drying and other processes to improve economic benefits. The traditional evaporation, concentration and cooling process has the following defects:

[0004] 1. The secondary steam generated in the front liquefaction section is directly discharged, which produces a large amount of white mist and puts great pressure on environmental protection. It is necessary to control and utilize the secondary flash steam to reduce energy consumption and improve the level of automation;

[0005] 2. The evaporation and concentration unit has high energy consumption and large amount of raw steam, which reduces the economic benefits of the product;

[0006] 3. The crystallization time of monohydrate crystalline sugar after concentration is relatively long, which normally takes about 60 hours. It requires multiple horizontal crystallizers and batch cooling crystallization. According to the calculation of 200TPD crystalline sugar, 42 30 cubic horizontal crystallizers are required. Batch production, large floor space, high construction cost, and cannot be produced continuously, and the labor force of workers is large. Utility Model Content

[0007] The purpose of this section is to summarize some aspects of the embodiments of the utility model and briefly introduce some preferred embodiments. Some simplifications or omissions may be made in this section and the specification abstract and utility model name of this application to avoid blurring the purpose of this section, specification abstract and utility model name, and such simplifications or omissions cannot be used to limit the scope of the utility model.

[0008] In view of the above problems and / or the problems existing in the prior art, the present utility model is proposed.

[0009] The utility model aims to overcome the problems existing in the prior art and provide a rice syrup evaporation, concentration and cooling device with low equipment investment, small floor space, high evaporation efficiency, good syrup quality and low production energy consumption.

[0010] In order to solve the above technical problems, the utility model provides a rice syrup evaporation, concentration and cooling device, comprising a saccharification liquid buffer tank, wherein the outlet of the saccharification liquid buffer tank is connected to the top inlet of a first-effect evaporator through a saccharification liquid delivery pump, the bottom outlet of the first-effect evaporator is connected to the top inlet of a secondary first-effect evaporator through a first-effect delivery pump, the bottom outlet of the secondary first-effect evaporator is connected to the top inlet of a second-effect evaporator through a secondary first-effect delivery pump, the bottom outlet of the second-effect evaporator is connected to the top inlet of a triple-effect evaporator through a second-effect delivery pump, and the bottom outlet of the triple-effect evaporator is connected to the top inlet of a vertical cooling crystallizer through a high-viscosity rotor pump;

[0011] The lower end of each effect evaporator is connected to a corresponding separator, the heat source inlet of the first effect evaporator is connected to the raw steam pipe, and the heat source inlet of the secondary first effect evaporator is connected to the gelatinization flash steam pipe; the secondary steam outlet of the first effect separator and the secondary first effect separator and the outlet of the saccharification flash steam pipe are connected to the heat source inlet of the second effect evaporator; the secondary steam outlet of the second effect separator is connected to the heat source inlet of the triple effect evaporator;

[0012] The secondary steam outlet of the three-effect separator and the non-condensable gas extraction port of each effect evaporator are connected to the shell side inlet of the condenser, and the shell side exhaust port of the condenser is connected to the atmosphere through a water ring vacuum pump.

[0013] As an improvement of the utility model, the condensed water outlets at the lower shell side of the first-effect evaporator and the secondary first-effect evaporator are connected to the lower shell side inlet of the second-effect evaporator through a water trap, the lower shell side outlet of the second-effect evaporator is connected to the lower shell side inlet of the three-effect evaporator through a water trap, and the lower shell side outlet of the three-effect evaporator is connected to the lower inlet of the evaporative condensed water tank.

[0014] As a further improvement of the utility model, the shell-side condensed water outlet of the condenser is connected to the lower inlet of the evaporative condensed water tank.

[0015] As a further improvement of the utility model, the water outlet of the evaporative condensate tank is connected to the inlet of the condensate output pump, and the outlet of the condensate output pump is connected to the process water pipe through a condensate regulating valve, and the opening of the condensate regulating valve is controlled by the liquid level of the evaporative condensate tank.

[0016] As a further improvement of the utility model, the non-condensable gas exhaust port of the secondary first effect evaporator is connected to the shell side inlet of the condenser through a secondary first effect non-condensable gas regulating valve, and a secondary first effect steam inlet pressure sensor is installed between the outlet of the gelatinization flash steam pipe and the heat source inlet of the secondary first effect evaporator, and the opening of the secondary first effect non-condensable gas regulating valve is controlled by the pressure measured by the secondary first effect steam inlet pressure sensor.

[0017] As a further improvement of the utility model, the raw steam pipe is connected to the heat source inlet of the first-effect evaporator through a first-effect steam inlet regulating valve. The heat source inlet of the first-effect evaporator is also equipped with a first-effect pressure sensor. The opening of the first-effect steam inlet regulating valve is controlled by the pressure measured by the first-effect pressure sensor.

[0018] As a further improvement of the utility model, the first-effect evaporator, the secondary first-effect evaporator, the second-effect evaporator and the third-effect evaporator are all falling film evaporators.

[0019] As a further improvement of the utility model, the outlet pipe of the high-viscosity rotor pump is installed with a mass flow meter and a pneumatic three-way valve in sequence, the main outlet of the pneumatic three-way valve is connected to the top inlet of the vertical cooling crystallizer, and the bypass outlet of the pneumatic three-way valve is connected to the inlet of the saccharification liquid delivery pump.

[0020] As a further improvement of the present invention, the outlet of each cooling coil of the vertical cooling crystallizer is respectively connected to the inlet of the corresponding partitioned cooling water tank, the outlet of each partitioned cooling water tank is respectively connected to the hot side inlet of the corresponding plate heat exchanger, the hot side outlet of each plate heat exchanger is respectively connected to the inlet of the corresponding partitioned cooling water pump, and the outlet of each partitioned cooling water pump is respectively connected to the inlet of the corresponding cooling coil.

[0021] As a further improvement of the present invention, the bottom outlet of the vertical cooling crystallizer is connected to a circulation valve and a discharge valve, the outlet of the circulation valve is connected to the top circulation port of the vertical cooling crystallizer through a crystallizer circulation pump and a circulation pipe; the outlet of the discharge valve is connected to the inlet of a sugar mass delivery pump.

[0022] Compared with the prior art, the utility model has achieved the following beneficial effects: 1. The secondary steam generated by gelatinization and saccharification in the liquefaction stage is directly used as a heat source for evaporation in the first-effect evaporator, thereby improving heat utilization efficiency and reducing steam consumption;

[0023] 2. Each evaporator uses a falling film evaporator. The saccharified liquid flows downward along the inner wall of each falling film tube, increasing the specific surface area of ​​the saccharified liquid and improving the heat exchange efficiency. The flash steam in the liquefaction section is used as the heat source of the evaporation system, which not only avoids the very eye-catching white fog phenomenon caused by external discharge, but also reduces the energy consumption of the evaporation system.

[0024] 3. Use vertical cooling crystallizers to cool accurately in different zones. According to the 200TPD crystal sugar production capacity, only six 178 cubic vertical cooling crystallizers are needed, which have a small footprint, low civil construction costs, cooling in different zones along the elevation, and continuous crystallization, and low labor intensity for workers;

[0025] 4. Liquefy broken rice starch to make crystal sugar, rationally utilize the effective ingredients in broken rice, and increase factory profits and product added value by saving energy and reducing consumption. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] In order to more clearly illustrate the technical solutions of the embodiments of the present utility model, the following will briefly introduce the drawings required for the description of the embodiments. Obviously, the drawings described below are only some embodiments of the present utility model. For ordinary technicians in this field, other drawings can be obtained based on these drawings without creative labor. The drawings are only provided for reference and explanation, not for limiting the present utility model. Among them:

[0027] Figure 1 This is a flow chart of the rice syrup evaporation concentration cooling device of the utility model;

[0028] In the figure: raw steam pipe 100; gelatinization flash steam pipe 200; saccharification flash steam pipe 300;

[0029] Saccharification liquid buffer tank 401; liquid level sensor LT401; saccharification liquid delivery pump 402; saccharification liquid flow meter FT402;

[0030] First-effect evaporator 4031; first-effect steam inlet regulating valve PC4031; first-effect pressure sensor PA4031; auxiliary first-effect evaporator 4032; auxiliary first-effect steam inlet pressure sensor PA4032; auxiliary first-effect non-condensable gas regulating valve PC4032; second-effect evaporator 4033; third-effect evaporator 4034;

[0031] The first effect separator 4041; the secondary first effect separator 4042; the second effect separator 4043; the third effect separator 4044;

[0032] First-effect delivery pump 4051; Secondary first-effect delivery pump 4052; Secondary effect delivery pump 4053; High viscosity rotor pump 4054; Mass flow meter DT4054; Pneumatic three-way valve KV401;

[0033] Evaporative condensate tank 406; condensate output pump 407; condensate regulating valve LC407; condenser 408; water ring vacuum pump 409;

[0034] Vertical cooling crystallizer 501; zone temperature sensor TT501; zone cooling water tank 502; zone cooling water pump 503; plate heat exchanger 504; crystallizer circulation pump 505; massecuite delivery pump 506;

[0035] Cooling water supply main pipe 600; cooling water return main pipe 700. DETAILED DESCRIPTION

[0036] In the following description of the utility model, the terms "upper", "lower", "front", "back", "left", "right", "inside", "outside", etc. indicate directions or positional relationships based on the directions or positional relationships shown in the accompanying drawings. They are only for the convenience of describing the utility model and simplifying the description, and do not mean that the device must have a specific direction.

[0037] In order to make the technical means, creative features, objectives and effects of the present invention easier to understand, the present invention is further described below with reference to specific figures. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of them.

[0038] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as those commonly understood by those skilled in the art of the present invention. The terms used in the specification of the present invention are only for the purpose of describing specific embodiments and are not intended to limit the present invention.

[0039] like Figure 1 As shown, the rice syrup evaporation, concentration and cooling device of the utility model comprises a saccharification liquid buffer tank 401, a saccharification liquid delivery pump 402, a first-effect evaporator 4031, a secondary first-effect evaporator 4032, a second-effect evaporator 4033, a third-effect evaporator 4034 and a vertical cooling crystallizer 501, wherein the first-effect evaporator 4031, the secondary first-effect evaporator 4032, the second-effect evaporator 4033 and the third-effect evaporator 4034 are all falling film evaporators.

[0040] The outlet of the saccharification liquid buffer tank 401 is connected to the top inlet of the first-effect evaporator 4031 through the saccharification liquid delivery pump 402, and after being distributed by the distributor, it flows downward evenly along the inner wall of each first-effect falling film tube. The heat source inlet of the first-effect evaporator 4031 is connected to the steam pipe 100. The bottom of the first-effect evaporator 4031 is connected to the first-effect separator 4041, and the first-effect concentrated liquid enters the first-effect separator 4041 for evaporation and separation.

[0041] The bottom outlet of the first-effect evaporator 4031 is connected to the top inlet of the secondary first-effect evaporator 4032 through the first-effect delivery pump 4051, and after being distributed by the distributor, it flows downward evenly along the inner wall of each secondary first-effect falling film tube. The heat source inlet of the secondary first-effect evaporator 4032 is connected to the gelatinization flash steam pipe 200, and the bottom of the secondary first-effect evaporator 4032 is connected to the secondary first-effect separator 4042, and the concentrated liquid of the secondary first-effect enters the secondary first-effect separator 4042 for evaporation and separation.

[0042] The bottom outlet of the secondary first effect evaporator 4032 is connected to the top inlet of the second effect evaporator 4033 through the secondary first effect delivery pump 4052, and after being distributed by the distributor, it flows downward evenly along the inner wall of each second effect falling film tube. The secondary steam outlet of the first effect separator 4041 and the secondary first effect separator 4042 and the outlet of the saccharification flash steam pipe 300 are connected to the heat source inlet of the second effect evaporator 4033. The bottom of the second effect separator 4043 is connected to the second effect evaporator 4033, and the second effect concentrated liquid enters the second effect separator 4043 for evaporation and separation.

[0043] The bottom outlet of the second-effect evaporator 4033 is connected to the top inlet of the triple-effect evaporator 4034 through the second-effect delivery pump 4053, and after being distributed by the distributor, it flows downward evenly along the inner wall of each triple-effect falling film tube. The secondary steam outlet of the second-effect separator 4043 is connected to the heat source inlet of the triple-effect evaporator 4034; the bottom of the triple-effect evaporator 4034 is connected to the triple-effect separator 4044, and the triple-effect concentrated liquid enters the triple-effect separator 4044 for evaporation and separation.

[0044] The secondary steam outlet of the triple-effect separator 4044 is connected to the shell side inlet of the condenser 408 , and the shell side exhaust port of the condenser 408 is connected to the atmosphere through a water ring vacuum pump 409 .

[0045] The non-condensable gas exhaust port of each effect evaporator is connected to the shell side inlet of the condenser 408 through a vacuum pipe, and the shell side outlet of the condenser 408 is connected to the water ring vacuum pump 409. The vacuum degree of the evaporation concentration system is achieved by the water ring vacuum pump 409.

[0046] A secondary first effect steam inlet pressure sensor PA4032 is installed between the outlet of the gelatinization flash steam pipe 200 and the heat source inlet of the secondary first effect evaporator 4032. The non-condensable gas extraction port of the secondary first effect evaporator 4032 is connected to the shell side inlet of the condenser 408 through the secondary first effect non-condensable gas regulating valve PC4032 and the secondary first effect vacuum pipe. The opening of the secondary first effect non-condensable gas regulating valve PC4032 is controlled by the pressure measured by the secondary first effect steam inlet pressure sensor PA4032. The vacuum degree of the secondary first effect evaporator 4032 can be accurately adjusted by the secondary first effect non-condensable gas regulating valve PC4032, so that both the vacuum degree of the secondary first effect and the flash evaporation temperature of the gelatinization section can be controlled.

[0047] The bottom outlet of the triple-effect evaporator 4034 is connected to the inlet of the high-viscosity rotor pump 4054. The outlet pipe of the high-viscosity rotor pump 4054 is installed with a mass flowmeter DT4054 and a pneumatic three-way valve KV401 in sequence. The main outlet of the pneumatic three-way valve KV401 is connected to the top inlet of the vertical cooling crystallizer 501, and the bypass outlet of the pneumatic three-way valve KV401 is connected to the inlet of the saccharification liquid delivery pump 402.

[0048] The refined saccharified liquid enters the saccharified liquid buffer tank 401. The saccharified liquid buffer tank 401 is equipped with a liquid level sensor LT401 for monitoring the liquid level of the buffer tank. The liquid level of the buffer tank is automatically linked with the speed and flow rate of the saccharified liquid delivery pump 402. When the liquid level is higher than the set value, the pump frequency automatically increases to increase the feed flow rate of the saccharified liquid delivery pump 402. The outlet of the saccharified liquid delivery pump 402 is equipped with a saccharified liquid flow meter FT402, which is used to measure the feed amount of the evaporator. The syrup is delivered to the top of the first-effect evaporator 4031 through the saccharified liquid delivery pump 402, and evenly enters each falling film tube through the distributor, flows downward along the inner wall of the tube to form a falling film and evaporates under heat. The heat source is the steam from the raw steam pipe 100.

[0049] A first-effect steam inlet regulating valve PC4031 can be provided between the raw steam pipe 100 and the heat source inlet of the first-effect evaporator 4031. A first-effect pressure sensor PA4031 is also installed at the heat source inlet of the first-effect evaporator 4031. The opening of the first-effect steam inlet regulating valve PC4031 is controlled by the pressure measured by the first-effect pressure sensor PA4031. The first-effect evaporation pressure is interlocked with the first-effect steam inlet regulating valve PC4031. When the first-effect evaporation pressure is lower than the set value, the opening of the first-effect steam inlet regulating valve PC4031 is automatically adjusted to increase the steam intake amount.

[0050] The syrup indirectly exchanges heat with the raw steam during the descent process, and the syrup is heated and evaporated to produce first-effect secondary steam, which is used as the heat source of the second-effect evaporator 4033. The concentration of the syrup after the first-effect evaporation is increased, and it is sent to the secondary first-effect evaporator 4032 through the first-effect delivery pump 4051 for further evaporation. The secondary first-effect evaporator 4032 uses the waste heat of the flash steam of the gelatinization section as the heat source.

[0051] The syrup discharged from the auxiliary first effect is sent to the second effect evaporator 4033 through the auxiliary first effect delivery pump 4052 for further evaporation. The second effect evaporation has three heat sources, one heat source is the secondary steam generated by the first effect evaporator 4031, another heat source is the secondary steam generated by the auxiliary first effect evaporator 4032, and another heat source is the flash steam of the saccharification section.

[0052] The syrup discharged from the second-effect evaporator is sent to the third-effect evaporator 4034 through the second-effect delivery pump 4053 for evaporation and discharge. Since the third-effect discharge has a high sugar concentration and high viscosity, it cannot be discharged by an ordinary centrifugal pump, so a high-viscosity rotor pump 4054 is used to transport the discharge. A mass flow meter DT4054 is installed on the discharge pipeline to detect the concentration of the syrup evaporated discharge.

[0053] When the discharge concentration is lower than the set value, the pneumatic three-way valve KV401 automatically switches to the reflux state, that is, refluxes to the inlet of the saccharification liquid delivery pump 402 to continue the circulation evaporation;

[0054] When the discharge concentration is consistent with the set concentration, the pneumatic three-way valve KV401 automatically switches to the discharge state and enters the vertical cooling crystallizer 501 for cooling.

[0055] When the discharge concentration is higher than the set value, the first-effect steam inlet regulating valve PC4031 will automatically reduce the valve opening appropriately to increase the vacuum degree of the first-effect evaporator 4031, thereby reducing the evaporation amount to achieve the balance of the evaporation system.

[0056] The condensed water at the bottom of the shell side of the first effect evaporator 4031 and the secondary first effect evaporator 4032 enters the bottom of the shell side of the second effect evaporator 4033 through the water trap for flash evaporation. The condensed water at the bottom of the shell side of the second effect evaporator 4033 enters the bottom of the shell side of the third effect evaporator 4034 through the water trap for flash evaporation. The condensed water discharged from the bottom of the shell side of the third effect evaporator 4034 enters the evaporation condensed water tank 406 for collection.

[0057] The water outlet of the evaporative condensed water tank 406 is connected to the inlet of the condensed water output pump 407, and the outlet of the condensed water output pump 407 is connected to the process water pipe through the condensed water regulating valve LC407.

[0058] The secondary steam generated by the triple-effect evaporation enters the shell side of the condenser 408 for heat exchange with the circulating water, and the secondary steam is condensed into water and collected in the evaporation condensate tank 406. This part of condensate has a low COD content and is sent out through the condensate output pump 407 as process water for reuse. The opening of the condensate regulating valve LC407 on the outlet pipe of the condensate output pump 407 is interlocked with the liquid level of the evaporation condensate tank 406.

[0059] The evaporated and concentrated syrup is fed into the upper part of the vertical cooling crystallizer 501 by the high viscosity rotor pump 4054 through the discharge port of the pneumatic three-way valve KV401, and the temperature is reduced in different zones during the flow from top to bottom. The inner cavity of the vertical cooling crystallizer 501 is evenly provided with multiple cooling units along the height direction, and each cooling unit is respectively provided with a cooling coil, a zoned cooling water tank 502, a zoned cooling water pump 503 and a plate heat exchanger 504, and the cold side inlet of each plate heat exchanger 504 is respectively connected to the cooling water supply main pipe 600, and the cold side outlet of each plate heat exchanger 504 is respectively connected to the cooling water return main pipe 700.

[0060] The outlet of each partitioned cooling water tank 502 is respectively connected to the hot side inlet of the corresponding plate heat exchanger 504, the hot side outlet of each plate heat exchanger 504 is respectively connected to the inlet of the corresponding partitioned cooling water pump 503, the outlet of each partitioned cooling water pump 503 is respectively connected to the inlet of the corresponding cooling coil, and the outlet of each cooling coil is respectively connected to the inlet of the corresponding partitioned cooling water tank 502.

[0061] Each cooling zone is provided with a zone temperature sensor TT501, and the syrup temperature value of each section is controlled by circulating coolant, and the circulating coolant can be softened water. The speed of the zone cooling water pump 503 in each section is linked to the syrup temperature measured by the corresponding zone temperature sensor TT501. When the syrup temperature is higher than the set value, the frequency and speed of the zone cooling water pump 503 are automatically increased to increase the flow into the cooling coil; when the syrup temperature is lower than the set value, the frequency and speed of the zone cooling water pump 503 are automatically reduced to reduce the flow into the cooling coil.

[0062] After the circulating coolant indirectly exchanges heat with the syrup in the cooling coil, the syrup is cooled, and the temperature of the circulating coolant increases, and enters the partitioned cooling water tank 502, and then enters the hot side of the plate heat exchanger 504, and exchanges heat with the circulating cooling water on the cold side to cool down.

[0063] The bottom outlet of the vertical cooling crystallizer 501 is connected to the inlet of the crystallizer circulation pump 505 through a circulation valve, and the outlet of the crystallizer circulation pump 505 is connected to the top circulation inlet of the vertical cooling crystallizer 501 through a crystallizer circulation pipe. If the crystallization effect of the sugar mass after cooling and crystallization does not meet the requirements, it will be circulated back to the top of the crystallization tank through the crystallizer circulation pump 505.

[0064] The bottom outlet of the vertical cooling crystallizer 501 is connected to the inlet of the massecuite delivery pump 506 through a discharge valve. The massecuite that meets the crystallization requirements enters the massecuite delivery pump 506 through the discharge valve and is delivered by the massecuite delivery pump 506.

[0065] The above description is only the preferred feasible embodiment of the utility model, which shows and describes the basic principle, main features and advantages of the utility model, but does not limit the scope of patent protection of the utility model. The technicians in this industry should understand that the utility model is not limited by the above embodiments. In addition to the above embodiments, the utility model can also have other implementation modes without departing from the spirit and scope of the utility model. The utility model will also have various changes and improvements. All technical solutions formed by equivalent replacement or equivalent transformation fall within the scope of protection required by the utility model. The scope of protection required by the utility model is defined by the attached claims and their equivalents. The technical features not described in the utility model can be achieved by or using existing technologies, which will not be repeated here.

Claims

1. A rice syrup evaporation concentration cooling device, comprising a saccharification liquid buffer tank (401), characterized in that: The outlet of the saccharified liquid buffer tank (401) is connected to the top inlet of the first-effect evaporator (4031) through the saccharified liquid delivery pump (402), the bottom outlet of the first-effect evaporator (4031) is connected to the top inlet of the secondary first-effect evaporator (4032) through the first-effect delivery pump (4051), the bottom outlet of the secondary first-effect evaporator (4032) is connected to the top inlet of the second-effect evaporator (4033) through the secondary first-effect delivery pump (4052), the bottom outlet of the second-effect evaporator (4033) is connected to the top inlet of the triple-effect evaporator (4034) through the second-effect delivery pump (4053), and the bottom outlet of the triple-effect evaporator (4034) is connected to the top inlet of the vertical cooling crystallizer (501) through the high-viscosity rotor pump (4054); The lower end of each effect evaporator is connected to a corresponding separator, the heat source inlet of the first effect evaporator (4031) is connected to the raw steam pipe (100), and the heat source inlet of the secondary first effect evaporator (4032) is connected to the gelatinization flash steam pipe (200); the secondary steam outlets of the first effect separator (4041) and the secondary first effect separator (4042) and the outlet of the saccharification flash steam pipe (300) are connected to the heat source inlet of the second effect evaporator (4033); the secondary steam outlet of the second effect separator (4043) is connected to the heat source inlet of the third effect evaporator (4034); The secondary steam outlet of the three-effect separator (4044) and the non-condensable gas extraction port of each effect evaporator are connected to the shell side inlet of the condenser (408), and the shell side exhaust port of the condenser (408) is connected to the atmosphere through a water ring vacuum pump (409).

2. The rice syrup evaporation, concentration and cooling device according to claim 1, characterized in that: The condensed water outlets at the lower shell side of the first-effect evaporator (4031) and the secondary first-effect evaporator (4032) are connected to the lower shell side inlet of the second-effect evaporator (4033) through a water trap, the lower shell side outlet of the second-effect evaporator (4033) is connected to the lower shell side inlet of the third-effect evaporator (4034) through a water trap, and the lower shell side outlet of the third-effect evaporator (4034) is connected to the lower inlet of the evaporative condensed water tank (406).

3. The rice syrup evaporation, concentration and cooling device according to claim 2, characterized in that: The shell-side condensed water outlet of the condenser (408) is connected to the lower inlet of the evaporative condensed water tank (406).

4. The rice syrup evaporation, concentration and cooling device according to claim 2, characterized in that: The water outlet of the evaporative condensate tank (406) is connected to the inlet of the condensate output pump (407), and the outlet of the condensate output pump (407) is connected to the process water pipe through the condensate regulating valve (LC407), and the opening of the condensate regulating valve (LC407) is controlled by the liquid level of the evaporative condensate tank (406).

5. The rice syrup evaporation concentration cooling device according to claim 1, characterized in that: The non-condensable gas exhaust port of the secondary first effect evaporator (4032) is connected to the shell side inlet of the condenser (408) through the secondary first effect non-condensable gas regulating valve (PC4032), and a secondary first effect steam inlet pressure sensor (PA4032) is installed between the outlet of the gelatinization flash steam pipe (200) and the heat source inlet of the secondary first effect evaporator (4032), and the opening of the secondary first effect non-condensable gas regulating valve (PC4032) is controlled by the pressure measured by the secondary first effect steam inlet pressure sensor (PA4032).

6. The rice syrup evaporation concentration cooling device according to claim 1, characterized in that: The raw steam pipe (100) is connected to the heat source inlet of the first-effect evaporator (4031) through a first-effect steam inlet regulating valve (PC4031). The heat source inlet of the first-effect evaporator (4031) is also equipped with a first-effect pressure sensor (PA4031). The opening of the first-effect steam inlet regulating valve (PC4031) is controlled by the pressure measured by the first-effect pressure sensor (PA4031).

7. The rice syrup evaporation concentration cooling device according to claim 1, characterized in that: The first-effect evaporator (4031), the secondary first-effect evaporator (4032), the second-effect evaporator (4033) and the third-effect evaporator (4034) are all falling film evaporators.

8. The rice syrup evaporation, concentration and cooling device according to claim 1, characterized in that: The outlet pipe of the high-viscosity rotor pump (4054) is installed with a mass flow meter (DT4054) and a pneumatic three-way valve (KV401) in sequence, the main outlet of the pneumatic three-way valve (KV401) is connected to the top inlet of the vertical cooling crystallizer (501), and the bypass outlet of the pneumatic three-way valve (KV401) is connected to the inlet of the saccharification liquid delivery pump (402).

9. The rice syrup evaporation, concentration and cooling device according to any one of claims 1 to 8, characterized in that: The outlets of the cooling coils of the vertical cooling crystallizer (501) are respectively connected to the inlets of the corresponding partitioned cooling water tanks (502), the outlets of the partitioned cooling water tanks (502) are respectively connected to the hot side inlets of the corresponding plate heat exchangers (504), the hot side outlets of the plate heat exchangers (504) are respectively connected to the inlets of the corresponding partitioned cooling water pumps (503), and the outlets of the partitioned cooling water pumps (503) are respectively connected to the inlets of the corresponding cooling coils.

10. The rice syrup evaporation, concentration and cooling device according to any one of claims 1 to 8, characterized in that: The bottom outlet of the vertical cooling crystallizer (501) is connected to a circulation valve and a discharge valve, and the outlet of the circulation valve is connected to the top circulation port of the vertical cooling crystallizer (501) through a crystallizer circulation pump (505) and a circulation pipe; the outlet of the discharge valve is connected to the inlet of a sugar massecuite delivery pump (506).

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