CN215939038U - Wheat starch water MVR evaporation concentration device - Google Patents
Wheat starch water MVR evaporation concentration device Download PDFInfo
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- CN215939038U CN215939038U CN202121934400.1U CN202121934400U CN215939038U CN 215939038 U CN215939038 U CN 215939038U CN 202121934400 U CN202121934400 U CN 202121934400U CN 215939038 U CN215939038 U CN 215939038U
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Abstract
A wheat starch water MVR evaporation concentration device is formed by connecting a steam compressor, a steam-water separation tank, a secondary separator, a secondary evaporator, a primary separator, a secondary preheater, a condenser, a drainage pump, a No. 1 circulating pump-5 circulating pump, a concentrated liquid tank, a concentrated slurry pump, a condensed liquid tank, a condensed liquid pump, a primary preheater, a vacuum pump, a feeding buffer tank, a pipeline valve and the like; the secondary evaporator adopts four groups of built-in forced circulation falling film evaporation, the front concentration and the rear concentration are separately concentrated, the effective evaporation area is fully exerted, the fixed switching and the countercurrent circulation can be realized, and the thick slurry group heat exchange tube is cleaned by dilute liquid, so that the scaling period of the evaporator is delayed; the low-temperature feeding liquid is preheated by high-temperature condensate water and tail gas to reach the boiling point for feeding, so that steam is saved; can be popularized and applied to the starch water concentration treatment industry or other low-temperature concentration industries.
Description
Technical Field
The utility model belongs to the technical field of starch water concentration devices or equipment, and particularly relates to a wheat starch water MVR evaporation concentration device.
Background
In industrial production, various processes and devices are adopted for the concentration of the wheat starch water, and the problems of easy foaming, easy gelatinization, extremely short equipment scaling period and high maintenance cost of starch in the wheat starch water concentration process are always the symptoms of concentration process devices.
Aiming at the problems which are easy to appear in the conventional wheat starch water concentration device, the device is scientifically and reasonably innovated in process and equipment, the problems which are easy to appear in the conventional wheat starch water concentration process are avoided, the device is more efficient, energy-saving, safe and stable, meanwhile, the device is strong in operability and high in automation degree, and the requirements of industrial production are met.
Disclosure of Invention
The utility model aims to overcome the defects of the prior art and provide the wheat starch water MVR evaporation and concentration device which has the advantages of delaying the scaling period of an evaporator, saving steam, having high automation degree, giving full play to the effective evaporation area, saving energy and having high efficiency.
The technical scheme for solving the technical problems is as follows: a wheat starch water MVR evaporation concentration device, the starch liquid of the starch liquid storage tank enters the feeding buffer tank, the starch liquid in the feeding buffer tank enters the basket filter through the feeding pump, the starch liquid passing through the basket filter sequentially passes through a primary preheater and a secondary preheater, finally enters the inlet pipeline of a No. 5 circulating pump, is sent to the top end of a primary evaporator by the No. 5 circulating pump, enters a primary separator after being heated in a tube pass, the material concentrated by the primary separator is sent into the inlet pipeline of the No. 1 circulating pump through a diversion pipeline of the No. 5 circulating pump, is sent to the top end of a secondary evaporator by the No. 1 circulating pump, enters a secondary separator after being heated by the secondary evaporator for final concentration, when the material concentration is reached, the materials are pumped into a concentrated liquid tank for temporary storage through a discharge diversion pipeline of a No. 4 circulating pump, and the materials in the concentrated liquid tank are discharged out of the system through a thick liquid pump and enter the next working section;
the secondary steam generated in the first-stage separator 4 and the second-stage separator 2 is discharged from the top of the separator and enters a steam-water separation tank 22, the condensed water separated in the steam-water separation tank 22 is sent into a condensed water tank 13 by a drainage pump 21, most of the condensed water in the condensed water tank 13 enters a first-stage preheater 11 through a condensed water pump 12 to be preheated and utilized and then is discharged out of the system, and a small part of the condensed water is used as cooling water of a steam compressor 1, the steam separated in the steam-water separation tank 22 enters a steam compressor 1 to be pressurized and then enters a first-stage evaporator 5 and a second-stage evaporator 3 shell pass to be used as a heat source to heat materials in the tube pass, and then enters the condensed water tank 13, the non-condensable gas and a small amount of the secondary steam generated in the first-stage evaporator 5 and the second-stage evaporator 3 sequentially pass through the second-stage preheater 6 and the condenser 7, the circulating cooling water of the condenser 7 comes from the outside and flows through the condenser shell pass, then is discharged out of the system, the secondary steam forms condensed water to enter the condensed water tank 13, the non-condensable gases are pumped out of the system by a vacuum pump 10.
The second-stage evaporator is divided into four evaporators, each evaporator is provided with a circulating pump, and materials are pumped to the top of the second-stage evaporator by the corresponding circulating pump in each small circulation.
In the secondary evaporator, materials are firstly heated in the secondary evaporator under the action of a No. 1 circulating pump, water is evaporated in a secondary separator, then the materials enter the secondary evaporator to be heated again under the action of a No. 2 circulating pump, the materials are concentrated in the secondary separator, then the materials enter the secondary evaporator to be heated under the action of a No. 3 circulating pump 7 and are concentrated in the secondary separator, and finally the materials enter the secondary evaporator to be heated under the action of a No. 4 circulating pump, and final thickening is carried out in the secondary separator.
A concentration tester is arranged on a discharge pipeline of the No. 4 circulating pump.
Compared with the prior art, the utility model has the following advantages:
1. the utility model adopts the technology of recompression and utilization of the secondary vapor, thereby saving energy;
2. the utility model adopts a tubular falling film evaporation process, thereby being high-efficient and energy-saving;
3. the utility model adopts two-stage evaporation, high and low concentration are separately concentrated, and the evaporation efficiency is high;
4. the two-stage evaporator adopts four groups of built-in forced circulation falling film evaporation, and the front concentration and the rear concentration are separately concentrated, so that the effective evaporation area is fully exerted, and the energy is saved and the efficiency is high;
5. four groups of forced circulation falling film evaporation are arranged in the secondary evaporator, so that fixed switching and countercurrent circulation can be realized, and the thick slurry group heat exchange tubes are cleaned by dilute liquid, so that the scaling period of the evaporator is prolonged.
6. The low-temperature feeding liquid is preheated by high-temperature condensate water and tail gas to reach the boiling point for feeding, so that steam is saved;
7. the utility model adopts DCS control, is stable and reliable and has high automation degree.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of the present invention.
In the figure: 1. a vapor compressor; 2. a secondary separator; 3. a secondary evaporator; 4. a first stage separator; 5. a secondary separator; 6. a secondary preheater; 7. a condenser; 8. a feed buffer tank; 9. a feed pump; 10. a vacuum pump; 11. a primary preheater; 12. a condensate pump; 13. a condensate tank; 14. a underflow pump; 15. a concentrated liquid tank; 16. no. 5 circulating pump; 17. no. 3 circulating pump; 18. no. 4 circulating pump; 19. circulating pump No. 1; 20. no. 2 circulating pump; 21. draining pump; 22. a steam-water separation tank.
Detailed Description
The present invention will be described in further detail with reference to the following drawings and examples, but the present invention is not limited to these examples.
Example 1
In fig. 1, a starch liquid in a starch liquid storage tank enters a feeding buffer tank 8, the starch liquid in the feeding buffer tank 8 enters a basket filter through a feeding pump 9, the starch liquid passing through the basket filter sequentially passes through a primary preheater 11 and a secondary preheater 6, and finally enters an inlet pipeline of a No. 5 circulating pump 16, the starch liquid is sent to the top end of a primary evaporator 5 through the No. 5 circulating pump 16, and then enters a primary separator 4 after being heated through a pipeline, a material concentrated by the primary separator 4 is sent to an inlet pipeline of a No. 1 circulating pump 19 through a diversion pipeline of the No. 5 circulating pump 16, and is sent to the top end of a secondary evaporator 3 through the No. 1 circulating pump 19, the secondary evaporator 3 of the embodiment is divided into four evaporators, each evaporator is provided with a circulating pump, and each small circulation pump pumps the material to the top of the secondary evaporator 3 through the corresponding circulating pump. Further, in the second-stage evaporator 3, the material is firstly heated in the second-stage evaporator 3 under the action of the No. 1 circulating pump 19, water is evaporated in the second-stage separator 2, then the material enters the second-stage evaporator 2 to be heated again under the action of the No. 2 circulating pump 20, the material is concentrated in the second-stage separator 2, then the material enters the second-stage evaporator 3 to be heated under the action of the No. 3 circulating pump 17, the material is concentrated in the second-stage separator 2, and finally the material enters the second-stage evaporator 3 to be heated under the action of the No. 4 circulating pump 18, and final thickening is carried out in the second-stage separator 2. Furthermore, the top of each evaporator is provided with a liquid distributor, so that the flowing materials are efficiently heated in a film forming distribution on the tubes. A concentration tester is arranged on the discharge pipeline of the No. 4 circulating pump 18, and the final concentration of the material is tested by the concentration tester to decide when to discharge the material. When reaching material concentration, the material is squeezed into concentrate jar 15 by 18 ejection of compact reposition of redundant personnel pipelines of circulating pump of No. 4 and is kept in, and the material in concentrate jar 15 is by the discharge system of underflow pump 14, gets into next workshop section.
The secondary steam generated in the first-stage separator 4 and the second-stage separator 2 is discharged from the top of the separator and enters a steam-water separation tank 22, the condensed water separated in the steam-water separation tank 22 is sent into a condensed water tank 13 by a drainage pump 21, most of the condensed water in the condensed water tank 13 enters a first-stage preheater 11 through a condensed water pump 12 to be preheated and utilized and then is discharged out of the system, and a small part of the condensed water is used as cooling water of a steam compressor 1, the steam separated in the steam-water separation tank 22 enters a steam compressor 1 to be pressurized and then enters a first-stage evaporator 5 and a second-stage evaporator 3 shell pass to be used as a heat source to heat materials in the tube pass, and then enters the condensed water tank 13, the non-condensable gas and a small amount of the secondary steam generated in the first-stage evaporator 5 and the second-stage evaporator 3 sequentially pass through the second-stage preheater 6 and the condenser 7, the circulating cooling water of the condenser 7 comes from the outside and flows through the condenser shell pass, then is discharged out of the system, the secondary steam forms condensed water to enter the condensed water tank 13, the non-condensable gases are pumped out of the system by a vacuum pump 10.
The working principle of the utility model is as follows:
first, material flow
1. Starch liquid (hereinafter referred to as material) from a starch liquid storage tank firstly reaches a feeding buffer tank 8, is conveyed by a feeding pump 9, is sequentially subjected to deslagging by a basket filter, is subjected to material temperature raising by a primary secondary preheater, finally enters an inlet pipeline of a No. 5 circulating pump 16 and enters a primary evaporation system.
2. In the primary evaporation system, materials are conveyed to the top end of a primary evaporator 5 by a No. 5 circulating pump 16, are uniformly distributed by a liquid distributor at the top of the evaporator, are efficiently heated in a film forming distribution on a tube array, flow heated by a tube pass flows to a primary separator 4, and moisture flashed from the materials is concentrated.
3. When the material after primary concentration in the primary evaporation system reaches the set concentration, the material is pumped into an inlet pipeline of a No. 1 circulating pump 19 through a diversion pipeline of a No. 5 circulating pump 16, and then enters the secondary evaporation system.
4. The secondary evaporator 3 is divided into four evaporators, each evaporator is provided with a circulating pump, each small circulation pump pumps materials to the top of the secondary evaporator 3, and the materials are uniformly distributed by the liquid distributor and are efficiently heated in a falling film mode.
5. In the second grade evaporation system, the material is at first under the effect of circulating pump 19 No. 1, is heated in second grade evaporimeter 3 to evaporate moisture in second grade separator 2, enter into second grade evaporimeter 2 under the effect of circulating pump 20 No. 2 and heat again subsequently, concentrate in second grade separator 2, later enter into second grade evaporimeter 3 and heat under the effect of circulating pump 17 No. 3, concentrate in second grade separator 2, the last material passes through circulating pump 18 No. 4, it is heated to get into second grade evaporimeter 3, carry out final densification in second grade separator 2.
6. The final concentration of material relies on the concentration measurement appearance of installing on 18 ejection of compact pipelines of circulating pump No. 4 to decide when to arrange the material, when material concentration reachd, the switch and the aperture of density control governing valve make qualified material in time get into concentrate tank 15 and keep in. The material level of each small circulation in the secondary evaporator 3 is adjusted by the discharge concentration and speed. In order to prevent the phenomenon of pipe blockage caused by discharging, when the concentration does not reach the standard, a front return pipeline of the regulating valve is arranged, and the smoothness of a discharging pipeline is ensured.
7. The final concentrated material (thick liquid) is discharged from the system by the thick liquid pump 14 and enters the next working section.
Second, steam and vacuum process
1. Because the MVR evaporation technology is adopted, only a small amount of fresh steam needs to be supplemented in the normal evaporation process, and the fresh steam comes from a boiler room;
2. when the device normally operates, secondary steam generated by the flash evaporation of heated materials in each separator is discharged from the top of the separator, enters the steam compressor 1 through an air inlet pipeline of the steam compressor 1, is pressurized by the steam compressor 1 and then enters the shell pass of each evaporator to serve as a heat source to heat the materials in the tube pass, and then condensed water is formed and enters a condensed water tank 13 to be discharged out of the system; noncondensable gas and a small amount of secondary steam enter and sequentially pass through the secondary preheater 6 and the condenser 7, wherein the secondary steam forms condensed water and is discharged to a condensed liquid tank 13; non-condensable gas is pumped out of the system by a vacuum pump 10, and the vacuum degree required by the system work is maintained;
third, condensed water flow
1. In each evaporator shell pass, condensed water formed by secondary steam automatically flows to a condensed liquid tank 13, and steam condensed water in the secondary preheater 6 and the condenser 7 also automatically flows to the condensed liquid tank 13;
2. the inlet pipeline of the steam compressor 1 is provided with a steam-water separation tank 22 to collect a small amount of condensed water in the secondary steam and prevent the condensed water from entering the steam compressor 1. The condensed water in the casing of the steam compressor 1 is collected by the drain tank of the steam compressor 1 and discharged to the steam-water separation tank 22. The condensed water in the steam-water separation tank 11 is sent into the condensed water tank 13 by the drainage pump 21; most of the condensed water in the condensed liquid tank 13 is discharged out of the system through the condensed liquid pump 12, and a small amount of the condensed water is used as cooling water of the vapor compressor 1 and enters the vapor compressor 1; the cold water discharged from the system flows through the primary preheater 11 to preheat the materials entering the system, and the heat of the materials is fully utilized.
Fourth, circulating cooling water and process water flow
1. Circulating cooling water of the condenser 7 comes from the outside, flows through the shell pass of the condenser 7, is discharged out of the system and is discharged to an external pipe network;
2. the process water, the cleaning water and the pump sealing water come from the outside.
Claims (4)
1. The utility model provides a wheat starch water MVR evaporation concentration device which characterized in that: starch liquid in a starch liquid storage tank enters a feeding buffer tank (8), the starch liquid in the feeding buffer tank (8) enters a basket filter through a feeding pump (9), the starch liquid passing through the basket filter sequentially passes through a primary preheater (11) and a secondary preheater (6), finally enters an inlet pipeline of a No. 5 circulating pump (16), the starch liquid is sent to the top end of a primary evaporator (5) through the No. 5 circulating pump (16), the starch liquid enters a primary separator (4) after being heated through a process, the material concentrated by the primary separator (4) is sent to the inlet pipeline of a No. 1 circulating pump (19) through a diversion pipeline of the No. 5 circulating pump (16), the starch liquid is sent to the top end of a secondary evaporator (3) through the No. 1 circulating pump (19), the starch liquid enters the secondary separator (2) after being heated through the secondary evaporator (3) to be finally concentrated, when the material concentration is reached, the material is sent to a concentrated liquid tank (15) for temporary storage through a discharge diversion pipeline of the No. 4 circulating pump (18), the material in the concentrated solution tank (15) is discharged out of the system by a thick slurry pump (14) and enters the next working section;
secondary steam generated in the primary separator (4) and the secondary separator (2) is discharged from the top of the separator and enters a steam-water separation tank (22), condensed water separated in the steam-water separation tank (22) is sent into a condensed water tank (13) by a drainage pump (21), most of the condensed water in the condensed water tank (13) enters a primary preheater (11) through a condensed water pump (12) to be discharged out of a system after being preheated and utilized, and a small part of the condensed water is used as cooling water of a steam compressor (1), steam separated by the steam-water separation tank (22) enters a steam compressor (1) to be pressurized and then enters a primary evaporator (5) and a secondary evaporator (3) shell pass as heat sources to heat materials in a pipe pass and then enters the condensed water tank (13), non-condensable gas and a small amount of secondary steam generated by the primary evaporator (5) and the secondary evaporator (3) sequentially pass through a secondary preheater (6) and a condenser (7), circulating cooling water of the condenser (7) comes from the outside, flows through the shell pass of the condenser and then is discharged out of the system, secondary steam forms condensed water which enters a condensed liquid tank (13), and non-condensable gas is pumped out of the system by a vacuum pump (10).
2. The wheat starch water MVR evaporation concentration device of claim 1, characterized in that: the secondary evaporator (3) is divided into four evaporators, each evaporator is provided with a circulating pump, and materials are pumped to the top of the secondary evaporator (3) by the corresponding circulating pump in each small circulation.
3. The wheat starch water MVR evaporation concentration device of claim 2, characterized in that: in the second-stage evaporator (3), materials are firstly heated in the second-stage evaporator (3) under the action of a No. 1 circulating pump (19), water is evaporated in the second-stage separator (2), then the materials enter the second-stage evaporator (3) to be heated again under the action of a No. 2 circulating pump (20), the materials are concentrated in the second-stage separator (2), then the materials enter the second-stage evaporator (3) to be heated under the action of a No. 3 circulating pump (17), the materials are concentrated in the second-stage separator (2), and finally the materials enter the second-stage evaporator (3) to be heated under the action of a No. 4 circulating pump (18), and final thickening is carried out in the second-stage separator (2).
4. The wheat starch water MVR evaporation concentration device of claim 3, characterized in that: and a concentration tester is arranged on the discharge pipeline of the No. 4 circulating pump (18).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121934400.1U CN215939038U (en) | 2021-08-17 | 2021-08-17 | Wheat starch water MVR evaporation concentration device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121934400.1U CN215939038U (en) | 2021-08-17 | 2021-08-17 | Wheat starch water MVR evaporation concentration device |
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| CN215939038U true CN215939038U (en) | 2022-03-04 |
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| CN202121934400.1U Active CN215939038U (en) | 2021-08-17 | 2021-08-17 | Wheat starch water MVR evaporation concentration device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114751476A (en) * | 2022-04-21 | 2022-07-15 | 启东神农机械有限公司 | Concentration process of wheat starch slurry and evaporation concentration system thereof |
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2021
- 2021-08-17 CN CN202121934400.1U patent/CN215939038U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114751476A (en) * | 2022-04-21 | 2022-07-15 | 启东神农机械有限公司 | Concentration process of wheat starch slurry and evaporation concentration system thereof |
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