CN103566612A - Compression heat pump rectification device and process - Google Patents
Compression heat pump rectification device and process Download PDFInfo
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- CN103566612A CN103566612A CN201210278258.9A CN201210278258A CN103566612A CN 103566612 A CN103566612 A CN 103566612A CN 201210278258 A CN201210278258 A CN 201210278258A CN 103566612 A CN103566612 A CN 103566612A
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- rectifying column
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/007—Energy recuperation; Heat pumps
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
- Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
- Y02B30/52—Heat recovery pumps, i.e. heat pump based systems or units able to transfer the thermal energy from one area of the premises or part of the facilities to a different one, improving the overall efficiency
Abstract
The invention belongs to the field of chemical engineering separation process and energy-saving technology and discloses a compression heat pump rectification device and a compression heat pump rectification process. The compression heat pump rectification device comprises a material feeding evaporator (1), a material feeding steam compressor (2), a rectification tower (3), a tower top condensation cooler (4) and a reflux tank (5) which are connected by a pipeline in sequence. The invention also provides the compression heat pump rectification process. Steam on the top of the rectification tower is a heat source for heating the feeding material, the feeding material can be heated to a dew point or above, the compression ratio of the tower top steam is remarkably reduced, the compression power consumption is reduced, and furthermore, the energy consumption is reduced.
Description
Technical field
The invention belongs to chemical separation process and field of energy-saving technology, relate to a kind of compression heat pump rectifier unit and technique.
Background technology
In chemical process, often relate to solvent and purify and separated rectification process process.In distillation process, directly by after overhead vapours condensation, partial condensation liquid refluxes as rectifying column conventionally, and part is as product extraction, and this kind of technique has not only increased cool cycles water consumption, and has lost the condensation latent heat of overhead vapours.Conventionally can adopt the compression heat-pump rectifying process such as outside working medium type, tower reactor Flash Type or overhead vapours direct vapor compression, reclaim tower top steam-condensation latent heat, such as propane-propylene separation, triphen separation etc.
Heat pump techniques is the new energy technology receiving much attention in the whole world in recent years.Heat pump is the device that a kind of heat energy by low-temperature heat source is transferred to high temperature heat source.As a kind of effective tool of UTILIZATION OF VESIDUAL HEAT IN, heat pump techniques is used in chemical industry rectifying field gradually.The people such as Supranto S. have studied and have related to two-stage both vapor compression, in the rectifier unit of separating alcohol and water, adopted heat pump distillation technology (Heat pump assisted distillation.IX:Acceptance trials on a system for separating ethanol and water, International Journal of Energy Research, 1988,12, p413-422).The people such as Gaspillo P. have introduced at dehydrogenation isopropanol reaction rectifying column and have adopted chemical heat pump distillation technology (Dehydrogenation of2-propanol in reactive distillation column for chemical heat pump, Journal of Chemical Engineering of Japan, 1998,31, p440-444).Chinese patent 200680023637.6 has been introduced a kind of rectifying device that uses heat pump, for the easy vaporization of rectifying aqueous mixture composition.
Chinese patent 200810231613.0 has been introduced diethyl carbonate heat pump distillation apparatus and technique, and rectifying tower top steam material is introduced after compressor pressurizes for tower reactor reboiler thermal source.The people such as Deng Renjie study butyl acetate heat pump distillation new technology (Chemical Engineering, 6 phases in 2006), for the high feature of conventional butyl acetate producing process energy consumption, propose that heat pump distillation is applied to butyl acetate and produce, develop butyl acetate heat pump distillation new technology.This technique equally by after overhead vapours compression for tower reactor reboiler thermal source, in device, the tower top tower reactor temperature difference of esterification column and rectifying column is respectively 13 ℃ and 18 ℃.
Heat pump techniques is applied to chemical industry rectification process, when the rectifying tower head tower still temperature difference is larger (while being particularly greater than 30 ℃), if adopt above-mentioned heat-pump rectifying process, exist compression ratio very high, cause the power of compressor to improve, energy-saving effect is not obvious, and using energy source is problem not fully.
Summary of the invention
In order to solve in chemical industry in heat-pump rectifying process, when the rectifying tower head tower still temperature difference is larger (while being particularly greater than 30 ℃), compression ratio is very high, and energy-saving effect is not obvious, and using energy source is problem not fully; The object of this invention is to provide a kind of compression heat pump rectifier unit.
Another object of the present invention is to provide a kind of compression heat pump rectification process.
Technical scheme of the present invention is as follows:
The invention provides a kind of compression heat pump rectifier unit, this device comprises charging evaporimeter, feed vapors compressor, rectifying column, overhead condensation cooler and backflash, connects successively through pipeline.
Described charging evaporimeter is provided with charging evaporation feed liquor mouth, charging evaporimeter discharging opening, charging evaporimeter heat medium charging aperture and charging evaporimeter heat medium discharging opening, charging evaporimeter heat medium charging aperture is positioned at the side of charging evaporimeter, and charging evaporimeter heat medium discharging opening is positioned at another corresponding side of charging evaporimeter heat medium charging aperture; Charging evaporimeter discharging opening is connected with compressor charging aperture, and charging evaporimeter heat medium discharging opening is connected with overhead condensation cooler charging aperture, and charging evaporimeter heat medium charging aperture is connected with rectifying column tower top steam (vapor) outlet.
Described feed vapors compressor is provided with compressor charging aperture and compressor discharging opening, and compressor charging aperture is connected with charging evaporimeter discharging opening, and compressor discharging opening is connected with rectifying column charging aperture.
Described rectifying column is provided with rectifying column charging aperture, rectifying column tower top steam (vapor) outlet, tower bottom of rectifying tower extraction mouth and phegma charging aperture, rectifying column charging aperture is positioned at the middle side edge of rectifying column, phegma charging aperture is positioned at another corresponding side of rectifying column charging aperture, rectifying column tower top steam (vapor) outlet is positioned at the top of rectifying column, and tower bottom of rectifying tower extraction mouth is positioned at the bottom of rectifying column; Rectifying column charging aperture is connected with compressor discharging opening, and rectifying column tower top steam (vapor) outlet is connected with charging evaporimeter heat medium charging aperture, and phegma charging aperture is connected with phegma outlet.
Described overhead condensation cooler is provided with cooler charging aperture and cooler discharging opening, and cooler charging aperture is connected with charging evaporimeter heat medium discharging opening, and cooler discharging opening is connected with backflash charging aperture.
Described backflash is provided with backflash charging aperture, phegma outlet and overhead product extraction mouth, and backflash charging aperture is connected with cooler discharging opening, and phegma outlet is connected with phegma charging aperture.
The present invention also provides a kind of compression heat pump rectification process, and this technique comprises the following steps:
First organic mixed solution to be separated is joined in charging evaporimeter, charging evaporimeter is heated to charging to vaporize completely as thermal source with rectifying column tower top steam under reduced pressure, and the charging after vaporization enters rectifying column after feed vapors compressor compresses improves feed pressure; Charging is after rectifying column rectifying, tower bottom of rectifying tower liquid reaches directly extraction after extraction standard, overhead vapours passes into charging evaporimeter and carries out heat exchange as thermal source, and the overhead vapours after heat exchange and partial condensation liquid enter overhead condensation cooler and is condensed into liquid and enters backflash; In backflash, condensate liquid partly passes into rectifying column continuation backflow, and all the other are as product extraction.
Described organic mixed solution is a kind of C
1～C
4the mixed liquor of organic compound and water or two kinds of C
1～C
4the mixed liquor of organic compound.
Described C
1～C
4organic compound is selected from alcohol, ketone, aldehyde or ester class organic compound, for example: methyl alcohol, ethanol, normal propyl alcohol, isopropyl alcohol, formaldehyde, acetaldehyde, propionic aldehyde, acetone, MEK, methyl formate or Ethyl formate.
The light component mass concentration of described organic mixed solution is 25 ~ 75%.
Described charging evaporimeter is selected from a kind of in plate type heat exchanger, pipe heat exchanger, tube-sheet heat exchanger or spiral heat exchanger, and heat transfer temperature difference scope is at 10 ~ 60 ℃.
Described feed vapors compressor is selected from positive displacement compressor, reciprocating compressor, and a kind of in centrifugal compressor, intensification scope is at 20 ~ 60 ℃, and compression ratio is 1.5 ~ 5.0.
Described rectifying column is selected from sieve-plate tower, a kind of in valve tower or packed tower, and overhead reflux ratio is 1.0 ~ 5.0.
Compared with the existing technology, tool has the following advantages and beneficial effect in the present invention:
1, the invention discloses a kind of Novel heat pump rectification process for the large temperature difference of tower top tower reactor (being greater than 30 ℃) rectifying, using rectifying tower top steam as the thermal source that adds hot feed, not only charging can be heated to dew point or above temperature, and obviously reduce the compression ratio of overhead vapours, reduce compression power consumption, thereby reduce energy resource consumption.
2, the present invention, by reclaiming the condensation latent heat of overhead vapours, effectively improves the required cool cycles water consumption that heating efficiency can greatly reduce overhead vapours condensation.
3, the present invention is applicable to the heat-pump rectifying process that all satisfy condition, and range of application is wide.
4, the present invention relates to a kind of compressing type heat-pump rectifying process of 30 ℃ that surpasses for the tower top tower reactor temperature difference.It is thermal source that this technique be take rectifying column tower top steam, and when charging being heated under reduced pressure to vaporization, overhead vapours is condensed.Charging after vaporization enters rectifying column after compressor compression.Compare with existing distillation technology, if the rectifying column of prior art adopts the gas-phase feed of external heat source heating, the present invention's vaporization institute consumption of calorie that economizes in raw materials; If the rectifying column of prior art is liquid phase feeding, the present invention transform rectifying column as gas-phase feed, because charging energy improves, and the energy consumption of greatly saving the needs of distillation process.For the large rectification process of traditional rectifying tower top tower reactor temperature difference, not only can save the cool cycles water consumption for condensing tower top steam, also the condensation latent heat of recyclable overhead vapours, improves heating efficiency, energy-saving and cost-reducing.
Accompanying drawing explanation
Fig. 1 represents the heat-pump rectifying process flow chart of the embodiment of the present invention.
1 is charging evaporimeter, 2 is feed vapors compressor, 3 is rectifying column, 4 is overhead condensation cooler, 5 is backflash, 11 is charging evaporation feed liquor mouth, 12 is charging evaporimeter discharging opening, 13 is charging evaporimeter heat medium charging aperture, 14 is charging evaporimeter heat medium discharging opening, 21 is compressor charging aperture, 22 is compressor discharging opening, 31 is rectifying column charging aperture, 32 is rectifying column tower top steam (vapor) outlet, 33 is tower bottom of rectifying tower extraction mouth, 34 is phegma charging aperture, 41 is cooler charging aperture, 42 is cooler discharging opening, 51 is backflash charging aperture, 52 is phegma outlet, 53 is overhead product extraction mouth.
Fig. 2 represents comparative example 1 conventional distillation process chart.
6 is that charging evaporimeter, 7 is that rectifying column, 8 is that overhead condensation cooler, 9 is backflash.
The specific embodiment
Below in conjunction with accompanying drawing illustrated embodiment, the present invention is further illustrated.
As shown in Figure 1, Fig. 1 represents the heat-pump rectifying process flow chart of the embodiment of the present invention to the flow process of 50wt% methanol-water solution separation process heat-pump rectifying process; Rectifying column adopts gas-phase feed.
According to inlet amount 10T/h, feeding temperature is 50 ℃ of calculating, rectifying column 3 adopts 45 actual plates, overhead reflux ratio is 3.0, thermal source using rectifying column 3 overhead extraction steam as charging evaporimeter 1, under reduced pressure, heating makes charging gasification, enters rectifying column 3 after then utilizing 2 compressions of feed vapors compressor to improve feed pressures.Rectifying column 3 tower tops obtain the methyl alcohol that water content is less than 100ppm, and in tower reactor extraction, methanol concentration is less than 100ppm equally.Overhead vapours after 1 heat exchange of charging evaporimeter is cooled to liquid phase in overhead condensation cooler 4, and heat exchange amount is 1.38Gcal/h.The heat exhaustion of rectifying column 3 tower reactor reboilers is 1.55Gcal/h.The liquid of overhead condensation cooler 4 condensations enters backflash 5; In backflash 5, condensate liquid partly passes into rectifying column 3 continuation backflows, and all the other are as product extraction.
Comparative example 1
As shown in Figure 2, rectifying column adopts gas-phase feed to 50wt% methanol-water solution separation process conventional distillation technique, inlet amount 10T/h, and feeding temperature is 50 ℃.
This distillation process adopts 45 actual plates, and rectifying column 7 overhead reflux ratios are 3.0, and tower top obtains the methyl alcohol that water content is less than 100ppm, and tower reactor extraction methanol concentration is less than 100ppm equally.According to inlet amount 10T/h, feeding temperature is 50 ℃ of calculating, and charging evaporimeter 6 is 4.43Gcal/h by the charging needed heat that is heated to gasify.Overhead condensation cooler 8 colds are 5.20Gcal/h.The heat exhaustion of rectifying column 7 tower reactor reboilers is 1.55Gcal/h.
Embodiment 2
As shown in Figure 1, rectifying column adopts gas-phase feed to the flow process of 25wt% ethanol-water solution separation process heat-pump rectifying process.
According to inlet amount 10T/h, feeding temperature is 50 ℃ of calculating, rectifying column 3 adopts 23 actual plates, overhead reflux ratio is 5.0, thermal source using rectifying column 3 overhead extraction steam as charging evaporimeter 1, under reduced pressure, heating makes charging gasification, enters rectifying column 3 after then utilizing 2 compressions of feed vapors compressor to improve feed pressures.Rectifying column 3 tower tops obtain the ethanol that water content is less than 15wt%, and tower reactor extraction concentration of alcohol is less than 0.5wt%.Overhead vapours after 1 heat exchange of charging evaporimeter is cooled to liquid phase in overhead condensation cooler 4, and heat exchange amount is 0.28Gcal/h.The heat exhaustion of rectifying column 3 tower reactor reboilers is 0.49Gcal/h.The liquid of overhead condensation cooler 4 condensations enters backflash 5; In backflash 5, condensate liquid partly passes into rectifying column 3 continuation backflows, and all the other are as product extraction.
Comparative example 2
As shown in Figure 2, rectifying column adopts gas-phase feed to 25wt% ethanol-water solution separation process conventional distillation technique, inlet amount 10T/h, and feeding temperature is 50 ℃.
This distillation process adopts 23 actual plates, and rectifying column 7 operating reflux ratios are 5.0, and tower top obtains the ethanol that water content is less than 15wt%, and tower reactor extraction concentration of alcohol is less than 0.5wt%.According to inlet amount 10T/h, feeding temperature is 50 ℃ of calculating, and charging evaporimeter 6 is 5.07Gcal/h by the charging needed heat that is heated to gasify.Overhead condensation cooler 8 colds are 5.17Gcal/h.The heat exhaustion of rectifying column 7 tower reactor reboilers is 0.49Gcal/h.
Embodiment 2 compares with comparative example 2, feed vapors compressor 2 is compressed to 1.5Bar(compression ratio 5.0 by feed vapors by about 0.3Bar), needed effective shaft power is 1050KW, according to electric efficiency 0.7, calculates, needing the power consumption increasing is 1500KW, i.e. 1.29Gcal/h.Whole technical process is saved heat energy and is consumed 5.07Gcal/h, saves cooling energy and consumes 4.89Gcal/h, adds up to and saves 8.67Gcal/h.
As shown in Figure 1, rectifying column adopts gas-phase feed to the flow process of 75wt% acetone-water solution separation process heat-pump rectifying process.
According to inlet amount 10T/h, feeding temperature is 50 ℃ of calculating, rectifying column 3 adopts 28 actual plates, overhead reflux ratio is 1.5, thermal source using rectifying column 3 overhead extraction steam as charging evaporimeter 1, under reduced pressure, heating makes charging gasification, enters rectifying column 3 after then utilizing 2 compressions of feed vapors compressor to improve feed pressures.Rectifying column 3 tower tops obtain the acetone that water content is less than 3wt%, and tower reactor extraction acetone concentration is less than 1wt%.Overhead vapours after 1 heat exchange of charging evaporimeter is cooled to liquid phase in overhead condensation cooler 4, and heat exchange amount is 0.31Gcal/h.The heat exhaustion of rectifying column 3 tower reactor reboilers is 0.37Gcal/h.The liquid of overhead condensation cooler 4 condensations enters backflash 5; In backflash 5, condensate liquid partly passes into rectifying column 3 continuation backflows, and all the other are as product extraction.
Comparative example 3
As shown in Figure 2, rectifying column adopts gas-phase feed to 75wt% acetone-water solution separation process conventional distillation technique, inlet amount 10T/h, and feeding temperature is 50 ℃.
This distillation process adopts 28 actual plates, and rectifying column 7 operating reflux ratios are 1.5, and tower top obtains the acetone that water content is less than 3wt%, and tower reactor extraction acetone concentration is less than 1wt%.According to inlet amount 10T/h, feeding temperature is 50 ℃ of calculating, and charging evaporimeter 6 is 2.63Gcal/h by the charging needed heat that is heated to gasify.Overhead condensation cooler 8 colds are 2.79Gcal/h.The heat exhaustion of rectifying column 7 tower reactor reboilers is 0.37Gcal/h.
As shown in Figure 1, Fig. 1 represents the heat-pump rectifying process flow chart of the embodiment of the present invention.
A rectifier unit, this device comprises charging evaporimeter 1, feed vapors compressor 2, rectifying column 3, overhead condensation cooler 4 and backflash 5, connects successively through pipeline.
Feed vapors compressor 2 is provided with compressor charging aperture 21 and compressor discharging opening 22, and compressor charging aperture 21 is connected with charging evaporimeter discharging opening 12, and compressor discharging opening 22 is connected with rectifying column charging aperture 31.
Rectifying column 3 is provided with rectifying column charging aperture 31, rectifying column tower top steam (vapor) outlet 32, tower bottom of rectifying tower extraction mouth 33 and phegma charging aperture 34, rectifying column charging aperture 31 is positioned at the middle side edge of rectifying column 3, phegma charging aperture 34 is positioned at another corresponding side of rectifying column charging aperture 31, rectifying column tower top steam (vapor) outlet 32 is positioned at the top of rectifying column 3, and tower bottom of rectifying tower extraction mouth 33 is positioned at the bottom of rectifying column 3; Rectifying column charging aperture 31 is connected with compressor discharging opening 22, and rectifying column tower top steam (vapor) outlet 32 is connected with charging evaporimeter heat medium charging aperture 13, and phegma charging aperture 34 is connected with phegma outlet 52.
The above-mentioned description to embodiment is can understand and apply the invention for ease of those skilled in the art.Person skilled in the art obviously can easily make various modifications to these embodiment, and General Principle described herein is applied in other embodiment and needn't passes through performing creative labour.Therefore, the invention is not restricted to the embodiment here, those skilled in the art are according to announcement of the present invention, and not departing from the improvement that category of the present invention makes and revise all should be within protection scope of the present invention.
Claims (13)
1. a compression heat pump rectifier unit, is characterized in that: this device comprises charging evaporimeter (1), feed vapors compressor (2), rectifying column (3), overhead condensation cooler (4) and backflash (5), connects successively through pipeline.
2. compression heat pump rectifier unit according to claim 1, it is characterized in that: described charging evaporimeter (1) is provided with charging evaporation feed liquor mouth (11), charging evaporimeter discharging opening (12), charging evaporimeter heat medium charging aperture (13) and charging evaporimeter heat medium discharging opening (14), charging evaporimeter heat medium charging aperture (13) is positioned at the side of charging evaporimeter (1), and charging evaporimeter heat medium discharging opening (14) is positioned at another corresponding side of charging evaporimeter heat medium charging aperture (13); Charging evaporimeter discharging opening (12) is connected with compressor charging aperture (21), charging evaporimeter heat medium discharging opening (14) is connected with overhead condensation cooler charging aperture (41), and charging evaporimeter heat medium charging aperture (13) is connected with rectifying column tower top steam (vapor) outlet (32).
3. compression heat pump rectifier unit according to claim 1, it is characterized in that: described feed vapors compressor (2) is provided with compressor charging aperture (21) and compressor discharging opening (22), compressor charging aperture (21) is connected with charging evaporimeter discharging opening (12), and compressor discharging opening (22) is connected with rectifying column charging aperture (31).
4. compression heat pump rectifier unit according to claim 1, it is characterized in that: described rectifying column (3) is provided with rectifying column charging aperture (31), rectifying column tower top steam (vapor) outlet (32), tower bottom of rectifying tower extraction mouth (33) and phegma charging aperture (34), rectifying column charging aperture (31) is positioned at the middle side edge of rectifying column (3), phegma charging aperture (34) is positioned at another corresponding side of rectifying column charging aperture (31), rectifying column tower top steam (vapor) outlet (32) is positioned at the top of rectifying column (3), tower bottom of rectifying tower extraction mouth (33) is positioned at the bottom of rectifying column (3), rectifying column charging aperture (31) is connected with compressor discharging opening (22), and rectifying column tower top steam (vapor) outlet (32) is connected with charging evaporimeter heat medium charging aperture (13), and phegma charging aperture (34) is connected with phegma outlet (52).
5. compression heat pump rectifier unit according to claim 1, it is characterized in that: described overhead condensation cooler (4) is provided with cooler charging aperture (41) and cooler discharging opening (42), cooler charging aperture (41) is connected with charging evaporimeter heat medium discharging opening (14), and cooler discharging opening (42) is connected with backflash charging aperture (51).
6. compression heat pump rectifier unit according to claim 1, it is characterized in that: described backflash (5) is provided with backflash charging aperture (51), phegma outlet (52) and overhead product extraction mouth (53), backflash charging aperture (51) is connected with cooler discharging opening (42), and phegma outlet (52) is connected with phegma charging aperture (34).
7. the compression heat pump rectification process that the arbitrary described device of claim 1 ~ 6 carries out, is characterized in that: this technique comprises the following steps:
First organic mixed solution to be separated is joined in charging evaporimeter (1), charging evaporimeter (1) is heated to charging to vaporize completely as thermal source with rectifying column (3) overhead vapours under reduced pressure, and the charging after vaporization enters rectifying column (3) after feed vapors compressor (2) compression improves feed pressure; Charging is after rectifying column (3) rectifying, rectifying column (3) tower reactor liquid reaches directly extraction after extraction standard, overhead vapours passes into charging evaporimeter (1) and carries out heat exchange as thermal source, and the overhead vapours after heat exchange and partial condensation liquid enter overhead condensation cooler (4) and is condensed into liquid and enters backflash (5); In backflash (5), condensate liquid partly passes into rectifying column (3) continuation backflow, and all the other are as product extraction.
8. compression heat pump rectification process according to claim 7, is characterized in that: described organic mixed solution is a kind of C
1～C
4the mixed liquor of organic compound and water or two kinds of C
1～C
4the mixed liquor of organic compound.
9. compression heat pump rectification process according to claim 8, is characterized in that: described C
1～C
4organic compound is selected from alcohol, ketone, aldehyde or ester class organic compound, for example: methyl alcohol, ethanol, normal propyl alcohol, isopropyl alcohol, formaldehyde, acetaldehyde, propionic aldehyde, acetone, MEK, methyl formate or Ethyl formate.
10. compression heat pump rectification process according to claim 7, is characterized in that: the light component mass concentration of described organic mixed solution is 25 ~ 75%.
11. compression heat pump rectification process according to claim 7, it is characterized in that: described charging evaporimeter (1) is selected from a kind of in plate type heat exchanger, pipe heat exchanger, tube-sheet heat exchanger or spiral heat exchanger, and heat transfer temperature difference scope is at 10 ~ 60 ℃.
12. compression heat pump rectification process according to claim 7, it is characterized in that: described feed vapors compressor (2) is selected from positive displacement compressor reciprocating compressor, a kind of in centrifugal compressor, intensification scope is at 20 ~ 60 ℃, and compression ratio is 1.5 ~ 5.0.
13. compression heat pump rectification process according to claim 7, is characterized in that: described rectifying column (3) is selected from a kind of in sieve-plate tower, valve tower or packed tower, and overhead reflux ratio is 1.0 ~ 5.0.
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| CN201210278258.9A CN103566612B (en) | 2012-08-06 | 2012-08-06 | A kind of compression heat pump rectifier unit and technique |
| PCT/CN2013/077862 WO2014023137A1 (en) | 2012-08-06 | 2013-06-25 | Compression-type heat pump assisted distillation device and process |
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| CN201210278258.9A CN103566612B (en) | 2012-08-06 | 2012-08-06 | A kind of compression heat pump rectifier unit and technique |
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| CN110156603A (en) * | 2019-04-12 | 2019-08-23 | 天津乐科节能科技有限公司 | A kind of method and device of dimethyl carbonate from backheat rectifying |
| CN114210081A (en) * | 2021-11-04 | 2022-03-22 | 湖北兴瑞硅材料有限公司 | Heat utilization process of organic silicon rectifying device |
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| CN105664517A (en) * | 2016-03-14 | 2016-06-15 | 江苏乐科节能科技股份有限公司 | Turbine and compressor combined heat pump rectification system and method |
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| CN107560233A (en) * | 2017-09-04 | 2018-01-09 | 江苏泰利达新材料股份有限公司 | A kind of alcohol heat pump distillation residual heat reutilizing system device |
| CN110156603A (en) * | 2019-04-12 | 2019-08-23 | 天津乐科节能科技有限公司 | A kind of method and device of dimethyl carbonate from backheat rectifying |
| CN114210081A (en) * | 2021-11-04 | 2022-03-22 | 湖北兴瑞硅材料有限公司 | Heat utilization process of organic silicon rectifying device |
| CN114307219A (en) * | 2022-02-23 | 2022-04-12 | 万华化学集团股份有限公司 | Method and equipment for rectifying and adjusting propylene rectifying tower and computer readable storage medium |
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| Publication number | Publication date |
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| WO2014023137A1 (en) | 2014-02-13 |
| CN103566612B (en) | 2015-12-02 |
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