CN212631775U - Negative pressure concentration total heat type evaporation recovery system - Google Patents
Negative pressure concentration total heat type evaporation recovery system Download PDFInfo
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- CN212631775U CN212631775U CN202022018502.0U CN202022018502U CN212631775U CN 212631775 U CN212631775 U CN 212631775U CN 202022018502 U CN202022018502 U CN 202022018502U CN 212631775 U CN212631775 U CN 212631775U
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Abstract
The utility model provides a concentrated total heat formula evaporation recovery system of negative pressure, it includes high temperature heat pump, air energy heat pump, circulation heat preservation heat storage box, heater, evaporimeter, preheating tank, condenser, plate heat exchanger and finished product ware, high temperature heat pump respectively with circulation heat preservation heat storage box and heater connection, the air energy heat pump is connected between high temperature heat pump and circulation heat preservation heat storage box, the heater is connected with evaporimeter and preheating tank, the evaporimeter is connected with condenser and finished product ware, preheating tank and plate heat exchanger and finished product ware are connected, plate heat exchanger is connected with the condenser, the condenser is connected with circulation heat preservation heat storage box. The utility model utilizes the reverse Carnot cycle principle to condense and recover the heat to be discharged in the concentration process, and then the heat is heated and used by the solution, thereby realizing the cyclic utilization of the heat, greatly reducing the energy consumption, having low evaporation boiling point and further reducing the energy consumption; the equipment is simple and efficient, a boiler is not needed, and a large amount of carbon emission and operation cost can be reduced.
Description
Technical Field
The utility model relates to a concentrated system field especially relates to a concentrated total heat type evaporation recovery system of negative pressure.
Background
The concentration process is widely used in the industries of pharmacy, chemical industry, food, environmental protection discharge and the like, and during the concentration process, most of water in the solution needs to be evaporated to obtain high-concentration solution, then the high-concentration solution is crystallized at low temperature, crystals are centrifuged out, and the finished product particles or finished product powder is obtained after drying.
The existing concentration process adopts normal pressure single-effect evaporation, negative pressure double-effect evaporation, negative pressure triple-effect evaporation or MVR evaporation. The negative pressure triple-effect evaporation equipment is large in size, complex in system and still incapable of opening a boiler, MVR evaporation is a concentration process with high heat utilization rate, a compressor is adopted by an MVR evaporator to improve the energy of secondary steam, the secondary steam with improved energy is utilized, and the latent heat of the secondary steam is recovered. The method specifically comprises the following steps: the secondary steam generated in the evaporator is compressed by the compressor in a heat insulation way, the pressure and the temperature of the secondary steam are increased, the secondary steam is used as heating steam and sent into a heating chamber of the evaporator, and finally the secondary steam is condensed to release heat and preheat feed liquid for use.
However, the MVR evaporation system works under a slight negative pressure during the working process, and does not actively obtain external energy, and the temperature in the evaporator gradually and slowly decreases during continuous operation, and still needs external steam to assist in the lifting; the evaporation boiling point is high, the temperature is about 100 ℃, the liquid is not suitable for heat-sensitive liquid materials, and in addition, the MVR equipment is large in investment, large in operation noise and high in maintenance cost; MVR evaporation still needs to dispose the boiler, still has fossil energy can increase the carbon emission problem, is unfavorable for the environmental protection.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a concentrated total heat formula evaporation recovery system of negative pressure to can not initiatively obtain external energy in solving prior art MVR evaporation system working process, temperature in the evaporimeter can progressively slow decline during the continuous operation, needs external steam to assist the promotion, and evaporation boiling point is high, and equipment drops into greatly, needs the problem of configuration boiler.
The utility model provides a negative pressure concentration total heat type evaporation recovery system, which comprises a high temperature heat pump, an air energy heat pump, a circulation heat preservation and storage box, a heater, an evaporator, a preheating tank, a condenser, a plate heat exchanger, a finished product device and a vacuum pump;
the high-temperature heat pump is connected with the circulating heat-preservation and heat-storage tank and the heater, and is used for efficiently absorbing heat recovered from the condenser by the circulating heat-preservation and heat-storage tank, supplying heat to the heater and heating feed liquid in the heater, wherein the outlet water temperature of the high-temperature heat pump is 75-90 ℃;
the air energy heat pump is connected between the high-temperature heat pump and the circulating heat-preservation and heat-storage tank and is used for preheating water in the circulating heat-preservation and heat-storage tank before work;
the circulating heat-preservation and heat-storage tank is connected with the condenser and is used for providing medium-temperature water for condensing secondary steam for the condenser and recovering the medium-temperature water after heat exchange in the condenser, and the temperature of the medium-temperature water is 30-45 ℃;
the heater is connected with the evaporator and the preheating tank and is used for heating feed liquid and providing high-temperature feed liquid for the evaporator;
the evaporator is connected with the heater, the condenser and the finished product device, and after the high-temperature heat pump carries out heat exchange type heating on the feed liquid in the heater, the evaporator obtains evaporated secondary steam under the combined action of the vacuum pump;
the preheating tank is connected with the plate heat exchanger and the finished product device and is used for exchanging heat with high-temperature concentrated liquid in the finished product device, reducing the temperature of the concentrated liquid in the finished product device, facilitating the crystallization of a later-stage process, recovering the heat of the high-temperature concentrated liquid in the finished product device and providing preheated liquid for the heater;
the plate heat exchanger is connected with the condenser and used for receiving medium-temperature water in the condenser and carrying out first-step preheating on the feed liquid in the preheating tank by using the received medium-temperature water;
and the vacuum pump is connected with the condenser and used for vacuumizing the heater and the evaporator to reduce the boiling point.
According to the utility model provides a concentrated total heat type evaporation recovery system of negative pressure has following beneficial effect:
the negative pressure concentration total heat type evaporation recovery system can recover a large amount of heat generated in the concentration process, and then the heat is used for heating the solution, so that the high-efficiency cyclic utilization of the heat is realized, the energy consumption is greatly reduced, the evaporation boiling point can be reduced, and the energy consumption is further reduced; the system has simple and efficient equipment, does not need a boiler, can greatly reduce carbon emission and operation cost, and has low equipment investment and operation and maintenance cost.
Additionally, according to the utility model provides a concentrated total heat type evaporation recovery system of negative pressure can also have following additional technical characterstic:
further, the high temperature heat pump with through first conveyer pipe and second duct connection between the heat storage box that circulates keeps warm, with through third conveyer pipe and fourth duct connection between the heater, be connected with a first motorised valve on the first conveyer pipe, be connected with a first circulating pump on the second conveyer pipe, be connected with a circulation delivery pump on the third conveyer pipe, the air energy heat pump is connected first conveyer pipe with on the second conveyer pipe.
Furthermore, the heater is connected with the evaporator through a fifth conveying pipe and a sixth conveying pipe, the heater is connected with the preheating tank through a seventh conveying pipe, the sixth conveying pipe is connected with a first material pump, and the seventh conveying pipe is connected with a one-way valve and a second material pump.
Furthermore, the evaporator is connected with the condenser through an eighth conveying pipe, and is connected with the finished product device through a ninth conveying pipe.
Furthermore, the preheating tank is connected with the finished product device through a tenth delivery pipe and an eleventh delivery pipe, the plate heat exchanger is connected with the plate heat exchanger through a twelfth delivery pipe and a thirteenth delivery pipe, the tenth delivery pipe is connected with a second electric valve, one end, close to the preheating tank, of the twelfth delivery pipe is connected to the eleventh delivery pipe, and a second circulating pump is connected to the position, close to the preheating tank, of the eleventh delivery pipe.
Furthermore, the condenser is connected with the circulation heat-preservation and heat-storage tank through a fourteenth conveying pipe and a fifteenth conveying pipe, the fourteenth conveying pipe is connected with a third circulation pump, and the fifteenth conveying pipe is connected with a third electric valve.
Further, the plate heat exchanger with through sixteenth conveyer pipe connection between the condenser, the sixteenth conveyer pipe is kept away from plate heat exchanger's one end is connected on the fifteenth conveyer pipe, the third motorised valve is close to circulation heat preservation heat-retaining case sets up.
Further, the condenser is connected with the vacuum pump through a vacuum pumping pipe.
Additional aspects and advantages of the invention will be set forth in part in the description which follows and, in part, will be obvious from the description, or may be learned by practice of the invention.
Drawings
The above and/or additional aspects and advantages of the present invention will become apparent and readily appreciated from the following description of the embodiments, taken in conjunction with the accompanying drawings of which:
fig. 1 is a schematic structural diagram of a negative pressure concentration total heat type evaporation recovery system according to an embodiment of the present invention;
fig. 2 is a schematic view of the operation cost of the negative pressure concentration total heat type evaporation recovery system of the embodiment of the present invention;
fig. 3 is a pressure enthalpy diagram of the R134a working medium of the negative pressure concentration total heat type evaporation recovery system of the embodiment of the present invention.
Reference numerals: 10. a high temperature heat pump; 11. an air-source heat pump; 12. a circulating heat preservation and storage tank; 13. a heater; 14. an evaporator; 15. a preheating tank; 16. a condenser; 17. a plate heat exchanger; 18. a finished product device; 19. a circulating delivery pump; 20. a first circulation pump; 21. a second circulation pump; 22. a third circulation pump; 23. A first material pump; 24. a second material pump; 25. a one-way valve; 26. a first electrically operated valve; 27. a second electrically operated valve; 28. a third electrically operated valve; 29. a vacuum pump.
Detailed Description
In order to make the objects, features and advantages of the present invention more comprehensible, embodiments of the present invention are described in detail below with reference to the accompanying drawings. Several embodiments of the invention are given in the accompanying drawings. The invention may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete.
Referring to fig. 1 to 3, an embodiment of the present invention provides a negative pressure concentrated total heat type evaporation recovery system, including a high temperature heat pump 10, an air energy heat pump 11, a circulation heat preservation and storage tank 12, a heater 13, an evaporator 14, a preheating tank 15, a condenser 16, a plate heat exchanger 17, a finisher 18, and a vacuum pump 29;
the high-temperature heat pump 10 is connected with the circulating heat-preservation and heat-storage tank 12 and the heater 13, and is used for efficiently absorbing heat recovered from the condenser 16 by the circulating heat-preservation and heat-storage tank 12, supplying heat to the heater 13, and heating feed liquid in the heater 13, wherein the outlet water temperature of the high-temperature heat pump is 75-90 ℃ (adjustable);
the air-source heat pump 11 is used for absorbing external energy (absorbing latent heat from air or other exhaust gas of an enterprise), is connected between the high-temperature heat pump 10 and the circulation heat-preservation heat storage tank 12, and is used for preheating water in the circulation heat-preservation heat storage tank 12 and supplementing heat before working;
the circulating heat-preservation and heat-storage tank 12 is connected with the condenser 16 and is used for providing medium-temperature water for condensing secondary steam for the condenser 16 and recovering the medium-temperature water subjected to heat exchange in the condenser 16, wherein the temperature of the medium-temperature water is 30-45 ℃;
the heater 13 is connected with the evaporator 14 and the preheating tank 15, and is used for heating the feed liquid and providing high-temperature feed liquid for the evaporator 14;
the evaporator 14 is connected with the heater 13, the condenser 16 and the finished product device 18, and after the feed liquid in the heater is subjected to heat exchange type heating through a high-temperature heat pump, the secondary steam obtained by evaporation is obtained under the combined action of a vacuum pump;
the preheating tank 15 is connected with the plate heat exchanger 17 and the finisher 18, and is used for exchanging heat with the high-temperature concentrated solution in the finisher 18, reducing the temperature of the concentrated solution in the finisher 18, facilitating crystallization, recovering the heat of the high-temperature concentrated solution in the finisher 18, and providing preheated feed liquid for the heater 13;
the plate heat exchanger 17 is connected with the condenser 16 and is used for receiving the medium-temperature water in the condenser 16 and preheating the feed liquid in the preheating tank 15 in the first step by using the received medium-temperature water;
and the vacuum pump 29 is connected with the condenser 16 and is used for vacuumizing the heater 13 and the evaporator 14 to reduce the boiling point.
High temperature heat pump 10 with through first conveyer pipe and second duct connection between the heat storage box 12 of circulation heat preservation, with through third conveyer pipe and fourth duct connection between the heater 13, be connected with a first motorised valve 26 on the first conveyer pipe, be connected with a first circulating pump 20 on the second conveyer pipe, be connected with a circulation delivery pump 19 on the third conveyer pipe, air energy heat pump 11 is connected first conveyer pipe with on the second conveyer pipe.
The heater 13 is connected with the evaporator 14 through a fifth delivery pipe and a sixth delivery pipe, and is connected with the preheating tank 15 through a seventh delivery pipe, the sixth delivery pipe is connected with a first material pump 23, and the seventh delivery pipe is connected with a one-way valve 25 and a second material pump 24.
The evaporator 14 is connected with the condenser 16 through an eighth delivery pipe, and is connected with the finisher 18 through a ninth delivery pipe.
The preheating tank 15 is connected with the finisher 18 through a tenth delivery pipe and an eleventh delivery pipe, the plate heat exchanger 17 is connected with the twelfth delivery pipe and a thirteenth delivery pipe, the tenth delivery pipe is connected with a second electric valve 27, one end of the twelfth delivery pipe close to the preheating tank 15 is connected with the eleventh delivery pipe, and a second circulating pump 21 is connected to the eleventh delivery pipe close to the preheating tank 15.
The condenser 16 is connected with the circulation heat-preservation and heat-storage tank 12 through a fourteenth delivery pipe and a fifteenth delivery pipe, the fourteenth delivery pipe is connected with a third circulation pump 22, and the fifteenth delivery pipe is connected with a third electric valve 28.
The utility model provides a pair of concentrated total heat formula evaporation recovery system of negative pressure's process flow:
a temperature rising stage: the first electric valve 26 is closed, the first circulating pump 20 is started at the moment, the air-source heat pump 11 (input power 45kw, heating capacity 135kw, maximum outlet water temperature 55 ℃, performance coefficient value of 3.0 at ambient temperature 15 ℃) is also started, and 20m is obtained within 4 hours3Liquid warms up to 50 ℃ (adjustable) back air energy heat pump stop motion in the heat storage box 12 of circulation heat preservation, this moment automatic open motorised valve 26 and high temperature heat pump 10, will simultaneously ammonium metatungstate aqueous solution pump in the preheater 15 heater 13 with evaporimeter 14, high temperature heat pump 10 begins to absorb sensible heat in the heat storage box 12 of circulation heat preservation does feed liquid heaies up in the heater 13.
A first concentration stage; when the feed liquid rises to behind 80 ℃ in the concentrated system (heater 13 with evaporimeter 14), opens vacuum pump 29 is to concentrated system evacuation, along with vacuum degree lower and lower, for example when vacuum degree reaches-70 kpa, water in the feed liquid just begins boiling evaporation at 70 ℃, the feed liquid is in high temperature heat pump 10 with circulation heating under the effect of first feed pump 23 (the highest leaving water temperature 85 ℃ of high temperature heat pump 10) to rise gradually to more than 75 ℃, feed liquid in evaporimeter 14 constantly produces 70 ℃ secondary steam and by vacuum pump 29 takes away evaporimeter 14, and the secondary steam that takes away cools off into 45 ℃ through water curtain condenser 16 rapidly (the cooling water by third circulating pump 22 drives), through secondary steam in the condenser 16 gives latent heat and sensible heat whole circulation heat preservation heat storage box 12, circulation heat preservation heat storage box 12 takes sensible heat through first circulating pump 20 again the water body give high temperature heat pump 10 Absorbing and entering full thermal cycle.
And (3) a second concentration stage: with the lapse of evaporation time, the water that condenses constantly gets into circulation heat preservation heat storage tank 12, when surpassing and setting for the liquid level value, third motorised valve 28 closes, and 50 ℃ of cooling water improves plate heat exchanger 17 with preheating tank 15 normal atmospheric temperature feed liquid carries out the heat transfer, and second circulating pump 21 starts this moment. At this time, the liquid level of the circulation heat-preservation and storage tank 12 also begins to drop, and when the liquid level is lower than the set liquid level, the third electric valve 28 is opened, the second circulation pump 21 is not closed, and the circulation is repeated.
The concentrated thick material is discharged from the evaporator 14 and enters the final product device 18 (with a stirring and jacket), the second electric valve 27 is opened, the feed liquid at 40 ℃ in the preheating tank 15 exchanges heat with the discharged thick material at 80 ℃ in the jacket of the final product device 18, on one hand, the feed liquid in the preheating tank 15 is heated to above 65 ℃, the feed liquid is preheated, on the other hand, the temperature of the thick material in the final product device 18 is reduced, and the next step of crystallization is facilitated. After the start, the second electrically operated valve 27 is always operated.
Referring to the pressure-enthalpy diagram of the R134a working medium in fig. 3, the following theoretical analysis is made:
evaporation of 1kg of water requires 600kc/kg of heat (including heat loss).
440 and 425 of 15kj/kg and 3.5851kc/kg working medium for compressor.
→ the overheated working medium steam (90 ℃) is cooled into saturated steam (80 ℃) which needs to release heat, i.e. 440-426-14 kj/kg-3.3460 kc/kg.
→ 426 and 320 parts by weight of working medium steam condensation heat release, 106 kj/kg.
④→⑤28kg/m3The throttling expansion of the working fluid is 15kg/m3Enthalpy was unchanged but 25% was vaporized.
→ 60 deg.C working fluid absorbs heat and vaporizes into saturated liquid, the heat absorption value is 425 and 320-105 kj/kg-25.095 kc/kg.
600kc/kg of heat power (including heat loss) is consumed for evaporating 1kg of water, or the heat of the 1kg of working medium can be released from 3.346+25.334 to 28.68kc, the water can be evaporated from 28.68/600 to 0.0478kg, and the power consumption is 3.5851kc/860 to 0.004169kwh (1kwh to 860kc) in each circulation.
The power consumption (1000/0.0478) × 0.004169 ═ 87.2kwh is required to evaporate 1000kg of water.
If the large electricity price is 0.7 yuan/kwh, it costs 87.2 x 0.7 ≈ 61 yuan to evaporate 1 ton of water.
The energy consumption for evaporating 1000kg of water by adopting steam heat power to negative pressure single effect is 66 kilocal, which is approximately equal to 1.1 steam ton and 0.4Mpa steam, and the energy consumption is 308 yuan calculated according to the steam price of 280 yuan/steam ton of a natural gas boiler.
To sum up, the utility model provides a pair of concentrated total heat type evaporation recovery system of negative pressure, beneficial effect lies in: this concentrated total-heat type evaporation recovery system of negative pressure can retrieve a large amount of heats that produce in the concentration process, supply the solution to heat again and use, realize thermal high-efficient cyclic utilization, greatly reduce the energy consumption, this concentrated total-heat type evaporation recovery system of negative pressure energy consumption is equivalent to n and imitates the evaporation, but save huge back end equipment (2 effects, 3 effects, 4 effect heating tank and evaporating pot, cooling tower etc.) input and area than n effect evaporation, and the equipment of this system is simple high-efficient, need not use the boiler, can greatly reduce the carbon emission and the working costs of fossil energy, equipment input and operation maintenance cost are low, this concentrated total-heat type evaporation recovery system of negative pressure still is fit for the evaporative concentration of heat sensitive material.
The above-mentioned embodiments only represent some embodiments of the present invention, and the description thereof is specific and detailed, but not to be construed as limiting the scope of the present invention. It should be noted that, for those skilled in the art, without departing from the spirit of the present invention, several variations and modifications can be made, which are within the scope of the present invention. Therefore, the protection scope of the present invention should be subject to the appended claims.
Claims (8)
1. A negative pressure concentration total heat type evaporation recovery system is characterized by comprising a high-temperature heat pump, an air energy heat pump, a circulation heat preservation and storage tank, a heater, an evaporator, a preheating tank, a condenser, a plate heat exchanger, a finished product device and a vacuum pump;
the high-temperature heat pump is connected with the circulating heat-preservation and heat-storage tank and the heater, and is used for efficiently absorbing heat recovered from the condenser by the circulating heat-preservation and heat-storage tank, supplying heat to the heater and heating feed liquid in the heater, wherein the outlet water temperature of the high-temperature heat pump is 75-90 ℃;
the air energy heat pump is connected between the high-temperature heat pump and the circulating heat-preservation and heat-storage tank and is used for preheating water in the circulating heat-preservation and heat-storage tank before work;
the circulating heat-preservation and heat-storage tank is connected with the condenser and is used for providing medium-temperature water for condensing secondary steam for the condenser and recovering the medium-temperature water after heat exchange in the condenser, and the temperature of the medium-temperature water is 30-45 ℃;
the heater is connected with the evaporator and the preheating tank and is used for heating feed liquid and providing high-temperature feed liquid for the evaporator;
the evaporator is connected with the heater, the condenser and the finished product device, and after the high-temperature heat pump carries out heat exchange type heating on the feed liquid in the heater, the evaporator obtains evaporated secondary steam under the combined action of the vacuum pump;
the preheating tank is connected with the plate heat exchanger and the finished product device and is used for exchanging heat with high-temperature concentrated liquid in the finished product device, reducing the temperature of the concentrated liquid in the finished product device, facilitating the crystallization of a later-stage process, recovering the heat of the high-temperature concentrated liquid in the finished product device and providing preheated liquid for the heater;
the plate heat exchanger is connected with the condenser and used for receiving medium-temperature water in the condenser and carrying out first-step preheating on the feed liquid in the preheating tank by using the received medium-temperature water;
and the vacuum pump is connected with the condenser and used for vacuumizing the heater and the evaporator to reduce the boiling point.
2. The negative-pressure concentrated total-heat type evaporation and recovery system according to claim 1, wherein the high-temperature heat pump is connected with the circulation heat-preservation and storage tank through a first delivery pipe and a second delivery pipe, and is connected with the heater through a third delivery pipe and a fourth delivery pipe, the first delivery pipe is connected with a first electric valve, the second delivery pipe is connected with a first circulating pump, the third delivery pipe is connected with a circulation delivery pump, and the air energy heat pump is connected with the first delivery pipe and the second delivery pipe.
3. The negative pressure concentration total heat type evaporation recovery system of claim 1, wherein the heater is connected with the evaporator through a fifth delivery pipe and a sixth delivery pipe, and is connected with the preheating tank through a seventh delivery pipe, the sixth delivery pipe is connected with a first material pump, and the seventh delivery pipe is connected with a one-way valve and a second material pump.
4. The negative pressure concentrating total heat type evaporation recovery system according to claim 1, wherein the evaporator is connected with the condenser through an eighth delivery pipe, and is connected with the final product device through a ninth delivery pipe.
5. The negative-pressure concentration total-heat type evaporation and recovery system according to claim 1, wherein the preheating tank is connected with the final product device through a tenth delivery pipe and an eleventh delivery pipe, the plate heat exchanger is connected with the plate heat exchanger through a twelfth delivery pipe and a thirteenth delivery pipe, a second electric valve is connected to the tenth delivery pipe, one end of the twelfth delivery pipe close to the preheating tank is connected to the eleventh delivery pipe, and a second circulating pump is connected to the eleventh delivery pipe close to the preheating tank.
6. The negative pressure concentration total heat type evaporation recovery system according to claim 1, wherein the condenser is connected with the circulation heat preservation and storage tank through a fourteenth delivery pipe and a fifteenth delivery pipe, the fourteenth delivery pipe is connected with a third circulation pump, and the fifteenth delivery pipe is connected with a third electric valve.
7. The negative pressure concentrated total heat type evaporation recovery system of claim 6, wherein the plate heat exchanger is connected with the condenser through a sixteenth delivery pipe, one end of the sixteenth delivery pipe, which is far away from the plate heat exchanger, is connected to the fifteenth delivery pipe, and the third electric valve is arranged close to the circulation heat preservation and storage tank.
8. The negative pressure concentrating total heat type evaporation recovery system of claim 1, wherein the condenser is connected with the vacuum pump through an evacuation pipe.
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| CN111974015A (en) * | 2020-09-15 | 2020-11-24 | 江西臻强新能源有限公司 | Negative pressure concentration total heat type evaporation recovery system |
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| CN111974015A (en) * | 2020-09-15 | 2020-11-24 | 江西臻强新能源有限公司 | Negative pressure concentration total heat type evaporation recovery system |
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