CN103566612B - A kind of compression heat pump rectifier unit and technique - Google Patents
A kind of compression heat pump rectifier unit and technique Download PDFInfo
- Publication number
- CN103566612B CN103566612B CN201210278258.9A CN201210278258A CN103566612B CN 103566612 B CN103566612 B CN 103566612B CN 201210278258 A CN201210278258 A CN 201210278258A CN 103566612 B CN103566612 B CN 103566612B
- Authority
- CN
- China
- Prior art keywords
- charging
- rectifying column
- evaporimeter
- charging aperture
- compressor
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- 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
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention belongs to chemical separation process and field of energy-saving technology, disclose a kind of compression heat pump rectifier unit and technique.The inventive system comprises charging evaporimeter (1), feed vapors compressor (2), rectifying column (3), overhead condensation cooler (4) and backflash (5), connect through pipeline successively.Present invention also offers a kind of compression heat pump rectification process.Charging as the thermal source adding hot feed, not only can be heated to dew point or more temperature by rectifying tower top steam by the present invention, and obviously reduces the compression ratio of overhead vapours, reduces compression power consumption, thus reduces energy resource consumption.
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 the rectification process process be separated.In distillation process, usually direct by after overhead vapours condensation, partial condensation liquid is as rectifier column reflux, and part is as product extraction, and this kind of technique not only adds cool cycles water consumption, and have lost the condensation latent heat of overhead vapours.Usually 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 is separated, triphen separation etc.
Heat pump techniques is the new energy technology received much attention in the whole world in recent years.Heat pump is a kind of by the device of the heat energy transfer of low-temperature heat source 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.SuprantoS. wait people have studied and relate to two-stage both vapor compression, heat pump distillation technology (Heatpumpassisteddistillation.IX:Acceptancetrialsonasyste mforseparatingethanolandwater is have employed in the rectifier unit of separating alcohol and water, InternationalJournalofEnergyResearch, 1988,12, p413-422).GaspilloP. wait people to describe and adopt chemical heat pump distillation technology (Dehydrogenationof2-propanolinreactivedistillationcolumnf orchemicalheatpump at dehydrogenation isopropanol reaction rectifying column, JournalofChemicalEngineeringofJapan, 1998,31, p440-444).Chinese patent 200680023637.6 describes a kind of rectifying device using heat pump, for composition of easily vaporizing in rectifying aqueous mixture.
Chinese patent 200810231613.0 describes diethyl carbonate heat pump distillation apparatus and technique, is used for tower reactor reboiler thermal source after rectifying tower top steam material is introduced compressor pressurizes.The people such as Deng Renjie study butyl acetate heat pump distillation new technology (Chemical Engineering, 6 phases in 2006), for the feature that conventional butyl acetate producing process energy consumption is high, propose heat pump distillation to be applied to butyl acetate and produce, develop butyl acetate heat pump distillation new technology.This technique is used for tower reactor reboiler thermal source after being compressed by overhead vapours equally, and in device, the tower top tower reactor temperature difference of esterification column and rectifying column is respectively 13 DEG C and 18 DEG C.
Heat pump techniques is applied to chemical industry rectification process, when the rectifying tower head tower still temperature difference is larger (when being particularly greater than 30 DEG C), if adopt above-mentioned heat-pump rectifying process, then there is compression ratio very high, the power of compressor is caused 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 (when being particularly greater than 30 DEG C), 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 exports with phegma and is connected.
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.
Present invention also offers a kind of compression heat pump rectification process, this technique comprises the following steps:
First organic mixed solution to be separated is joined in charging evaporimeter, charging is heated to vaporize completely as thermal source with rectifying column overhead vapours by charging evaporimeter at reduced pressure conditions, and the charging after vaporization enters rectifying column after feed vapors compressor compresses raising feed pressure; Charging is after rectifying column rectifying, tower bottom of rectifying tower liquid is direct extraction after reaching 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 part 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, such as: 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 the one 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 DEG C.
Described feed vapors compressor is selected from positive displacement compressor, reciprocating compressor, the one in centrifugal compressor, and temperature elevating range is at 20 ~ 60 DEG C, and compression ratio is 1.5 ~ 5.0.
Described rectifying column is selected from sieve-plate tower, and the one in valve tower or packed tower, 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 DEG C) rectifying, using rectifying tower top steam as the thermal source adding hot feed, not only charging can be heated to dew point or more temperature, and obviously reduce the compression ratio of overhead vapours, reduce compression power consumption, thus reduce energy resource consumption.
2, the present invention is 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 for the compressing type heat-pump rectifying process of the tower top tower reactor temperature difference more than 30 DEG C.This technique is with rectifying column overhead vapours for thermal source, and while charging being heated at reduced pressure conditions 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 then economizes in raw materials vaporization institute consumption of calorie; 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, greatly saves the energy consumption of the needs of distillation process.For the rectification process that traditional rectifying tower top tower reactor temperature difference is large, not only can save the cool cycles water consumption for condensing overhead vapor, also the condensation latent heat of recyclable overhead vapours, improve 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 for charging evaporimeter, 7 be rectifying column, 8 for overhead condensation cooler, 9 be backflash.
Detailed description of the invention
Below in conjunction with accompanying drawing illustrated embodiment, the present invention is further illustrated.
Embodiment 1
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 DEG C of calculating, rectifying column 3 adopts 45 pieces of actual plates, overhead reflux ratio is 3.0, using the thermal source of rectifying column 3 overhead extraction steam as charging evaporimeter 1, heating makes feed vaporization at reduced pressure conditions, enters rectifying column 3 after then utilizing feed vapors compressor 2 to compress raising feed pressure.Rectifying column 3 tower top obtains 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 charging evaporimeter 1 heat exchange 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 reboiler is 1.55Gcal/h.The liquid of overhead condensation cooler 4 condensation enters backflash 5; In backflash 5, condensate liquid part passes into rectifying column 3 continuation backflow, 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, and inlet amount 10T/h, feeding temperature is 50 DEG C.
This distillation process adopts 45 pieces of actual plates, and rectifying column 7 overhead reflux ratio is 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 DEG C of calculating, and the heat that charging is heated to required for gasification by charging evaporimeter 6 is 4.43Gcal/h.Overhead condensation cooler 8 cold is 5.20Gcal/h.The heat exhaustion of rectifying column 7 tower reactor reboiler is 1.55Gcal/h.
Embodiment 1 is compared with comparative example 1, feed vapors is compressed to 1.3Bar(compression ratio 4.3 by about 0.3Bar by feed vapors compressor 2), required effective shaft power is 793KW, calculates according to electric efficiency 0.7, the power consumption increased is needed to be 1135KW, i.e. 0.98Gcal/h.Whole technical process is saved heat energy and is consumed 4.43Gcal/h, saves cooling energy and consumes 3.82Gcal/h, add up to and save 7.27Gcal/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 DEG C of calculating, rectifying column 3 adopts 23 pieces of actual plates, overhead reflux ratio is 5.0, using the thermal source of rectifying column 3 overhead extraction steam as charging evaporimeter 1, heating makes feed vaporization at reduced pressure conditions, enters rectifying column 3 after then utilizing feed vapors compressor 2 to compress raising feed pressure.Rectifying column 3 tower top obtains the ethanol that water content is less than 15wt%, and tower reactor extraction concentration of alcohol is less than 0.5wt%.Overhead vapours after charging evaporimeter 1 heat exchange 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 reboiler is 0.49Gcal/h.The liquid of overhead condensation cooler 4 condensation enters backflash 5; In backflash 5, condensate liquid part passes into rectifying column 3 continuation backflow, 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, and inlet amount 10T/h, feeding temperature is 50 DEG C.
This distillation process adopts 23 pieces of actual plates, and rectifying column 7 operating reflux ratio is 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 DEG C of calculating, and the heat that charging is heated to required for gasification by charging evaporimeter 6 is 5.07Gcal/h.Overhead condensation cooler 8 cold is 5.17Gcal/h.The heat exhaustion of rectifying column 7 tower reactor reboiler is 0.49Gcal/h.
Embodiment 2 is compared with comparative example 2, feed vapors is compressed to 1.5Bar(compression ratio 5.0 by about 0.3Bar by feed vapors compressor 2), required effective shaft power is 1050KW, calculates according to electric efficiency 0.7, the power consumption increased is needed to be 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, add up to and save 8.67Gcal/h.
Embodiment 3
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 DEG C of calculating, rectifying column 3 adopts 28 pieces of actual plates, overhead reflux ratio is 1.5, using the thermal source of rectifying column 3 overhead extraction steam as charging evaporimeter 1, heating makes feed vaporization at reduced pressure conditions, enters rectifying column 3 after then utilizing feed vapors compressor 2 to compress raising feed pressure.Rectifying column 3 tower top obtains the acetone that water content is less than 3wt%, and tower reactor extraction acetone concentration is less than 1wt%.Overhead vapours after charging evaporimeter 1 heat exchange 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 reboiler is 0.37Gcal/h.The liquid of overhead condensation cooler 4 condensation enters backflash 5; In backflash 5, condensate liquid part passes into rectifying column 3 continuation backflow, 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, and inlet amount 10T/h, feeding temperature is 50 DEG C.
This distillation process adopts 28 pieces of actual plates, and rectifying column 7 operating reflux ratio is 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 DEG C of calculating, and the heat that charging is heated to required for gasification by charging evaporimeter 6 is 2.63Gcal/h.Overhead condensation cooler 8 cold is 2.79Gcal/h.The heat exhaustion of rectifying column 7 tower reactor reboiler is 0.37Gcal/h.
Embodiment 3 is compared with comparative example 3, feed vapors is compressed to 1.3Bar(compression ratio 3.7 by about 0.35Bar by feed vapors compressor 2), required effective shaft power is 620KW, calculates according to electric efficiency 0.7, the power consumption increased is needed to be 886KW, i.e. 0.76Gcal/h.Whole technical process is saved heat energy and is consumed 2.63Gcal/h, saves cooling energy and consumes 2.48Gcal/h, add up to and save 4.35Gcal/h.
Embodiment 4
As shown in Figure 1, Fig. 1 represents the heat-pump rectifying process flow chart of the embodiment of the present invention.
A kind of compression heat pump 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.
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, and 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.
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 and phegma export 52 and be connected.
Overhead condensation cooler 4 is provided with cooler charging aperture 41 and cooler discharging opening 42, and 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.
Backflash 5 is provided with backflash charging aperture 51, phegma outlet 52 and overhead product extraction mouth 53, and backflash charging aperture 51 is connected with cooler discharging opening 42, and phegma outlet 52 is connected with phegma charging aperture 34.
Above-mentioned is can understand and apply the invention for ease of those skilled in the art to the description of embodiment.Person skilled in the art obviously easily can make various amendment to these embodiments, and General Principle described herein is applied in other embodiments and need not through performing creative labour.Therefore, the invention is not restricted to embodiment here, those skilled in the art, according to announcement of the present invention, do not depart from improvement that scope makes and amendment all should within protection scope of the present invention.
Claims (8)
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;
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);
Described feed vapors compressor (2) is provided with compressor charging aperture (21) and compressor discharging opening (22);
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);
Described overhead condensation cooler (4) is provided with cooler charging aperture (41) and cooler discharging opening (42);
Described backflash (5) is provided with backflash charging aperture (51), phegma outlet (52) and overhead product extraction mouth (53);
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), and charging evaporimeter heat medium discharging opening (14) is connected with overhead condensation cooler charging aperture (41);
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 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), rectifying column tower top steam (vapor) outlet (32) is connected with charging evaporimeter heat medium charging aperture (13), and phegma charging aperture (34) exports (52) and is connected with phegma;
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);
Backflash charging aperture (51) is connected with cooler discharging opening (42), and phegma outlet (52) is connected with phegma charging aperture (34);
Charging is heated to vaporize completely as thermal source with rectifying column (3) overhead vapours by charging evaporimeter (1) at reduced pressure conditions;
Charging after vaporization enters rectifying column after feed vapors compressor (2) compression improves feed pressure.
2. the compression heat pump rectification process that carries out of device according to claim 1, is characterized in that: this technique comprises the following steps:
First organic mixed solution to be separated is joined in charging evaporimeter (1), charging is heated to vaporize completely as thermal source with rectifying column (3) overhead vapours by charging evaporimeter (1) at reduced pressure conditions, 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 is direct extraction after reaching 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 part passes into rectifying column (3) continuation backflow, and all the other are as product extraction.
3. compression heat pump rectification process according to claim 2, 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.
4. compression heat pump rectification process according to claim 3, is characterized in that: described C
1~ C
4organic compound is selected from alcohol, ketone, aldehyde or ester class organic compound, is selected from methyl alcohol, ethanol, normal propyl alcohol, isopropyl alcohol, formaldehyde, acetaldehyde, propionic aldehyde, acetone, MEK, methyl formate or Ethyl formate.
5. compression heat pump rectification process according to claim 2, is characterized in that: the light component mass concentration of described organic mixed solution is 25 ~ 75%.
6. compression heat pump rectification process according to claim 2, is characterized in that: described charging evaporimeter (1) is selected from 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 DEG C.
7. compression heat pump rectification process according to claim 2, it is characterized in that: described feed vapors compressor (2) is selected from the one in positive displacement compressor, reciprocating compressor and centrifugal compressor, temperature elevating range is at 20 ~ 60 DEG C, and compression ratio is 1.5 ~ 5.0.
8. compression heat pump rectification process according to claim 2, is characterized in that: described rectifying column (3) is selected from sieve-plate tower, valve tower or packed tower, and overhead reflux ratio is 1.0 ~ 5.0.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| 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 |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210278258.9A CN103566612B (en) | 2012-08-06 | 2012-08-06 | A kind of compression heat pump rectifier unit and technique |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103566612A CN103566612A (en) | 2014-02-12 |
| CN103566612B true CN103566612B (en) | 2015-12-02 |
Family
ID=50039856
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210278258.9A Active CN103566612B (en) | 2012-08-06 | 2012-08-06 | A kind of compression heat pump rectifier unit and technique |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN103566612B (en) |
| WO (1) | WO2014023137A1 (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN106542965B (en) * | 2016-11-07 | 2019-07-16 | 青岛科技大学 | The method of low carbon mixed alcohol tower reactor flash separation methanol |
| 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 |
| CN114307219B (en) * | 2022-02-23 | 2023-03-17 | 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 |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101357890A (en) * | 2008-09-17 | 2009-02-04 | 西安交通大学 | Methyl carbonate synthesis and refining technique using heat pump technique and apparatus thereof |
| CN101874935A (en) * | 2010-07-05 | 2010-11-03 | 天津大学 | Rectifying section tower bottom reboiling internal heat-integrated energy-saving rectifying apparatus and method |
| CN102583395A (en) * | 2012-03-15 | 2012-07-18 | 华陆工程科技有限责任公司 | Heat pump rectification method for refining trichlorosilane |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8002952B2 (en) * | 2007-11-02 | 2011-08-23 | Uop Llc | Heat pump distillation |
| CN101367733B (en) * | 2008-10-08 | 2011-12-07 | 西安交通大学 | Heat pump distillation apparatus and process for diethyl carbonate |
| CN102503016B (en) * | 2011-12-19 | 2013-09-04 | 杭州浙大合力科技有限公司 | Device and method for treating ammonia nitrogen wastewater, recycling ammonia and preparing ammonium sulfate |
-
2012
- 2012-08-06 CN CN201210278258.9A patent/CN103566612B/en active Active
-
2013
- 2013-06-25 WO PCT/CN2013/077862 patent/WO2014023137A1/en active Application Filing
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101357890A (en) * | 2008-09-17 | 2009-02-04 | 西安交通大学 | Methyl carbonate synthesis and refining technique using heat pump technique and apparatus thereof |
| CN101874935A (en) * | 2010-07-05 | 2010-11-03 | 天津大学 | Rectifying section tower bottom reboiling internal heat-integrated energy-saving rectifying apparatus and method |
| CN102583395A (en) * | 2012-03-15 | 2012-07-18 | 华陆工程科技有限责任公司 | Heat pump rectification method for refining trichlorosilane |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2014023137A1 (en) | 2014-02-13 |
| CN103566612A (en) | 2014-02-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103566613B (en) | A kind of low-concentration organic solvent aqueous solution reclaims heat pump distillation apparatus and technique | |
| CN103566612B (en) | A kind of compression heat pump rectifier unit and technique | |
| CN102875329B (en) | A kind of heat pump distillation is separated technique and the device of primary isoamyl alcohol isomers | |
| CN100584421C (en) | Differential pressure low-energy-consumption distillation method and equipment | |
| CN101874935B (en) | Rectifying section tower bottom reboiling internal heat-integrated energy-saving rectifying apparatus and method | |
| CN106431835B (en) | Process for separating ethanol-water by differential pressure thermal coupling rectification | |
| CN101195561B (en) | Method for producing dimethyl ether with methanol gas-phase dehydration | |
| CN109876485A (en) | Acetic acid recovery is from backheat rectifier unit and method | |
| CN101734999A (en) | Method for sequential separation and azeotropic recovery of ethyl benzene/styrene | |
| CN110105216B (en) | Self-backheating rectification method and device | |
| CN100412051C (en) | Heat pump rectifying prodn. process and plant for n-butyl acetate | |
| CN103086854B (en) | Method and device for reducing methanol content in formaldehyde process by silver method | |
| CN203677978U (en) | Vapor-compression type alcohol recovery tower | |
| CN210214856U (en) | Energy-efficient surplus aqueous ammonia distillation plant | |
| CN205323257U (en) | Ethanol differential pressure distillation plant with flash distillation | |
| CN110156603A (en) | A kind of method and device of dimethyl carbonate from backheat rectifying | |
| CN105964007A (en) | Equipment and process for separating n-butyl alcohol-isobutyl alcohol mixture | |
| CN104606910A (en) | Heat pump rectifying device based on heat storage technology and starting method of heat pump rectifying device | |
| CN108079610B (en) | Energy-saving methanol rectifying device and rectifying method thereof | |
| CN209836040U (en) | Potassium tert-butoxide indirect compression self-backheating rectification system | |
| CN207950711U (en) | Energy-saving methanol rectifying system | |
| CN201737865U (en) | Furfural production surplus heat utilization system | |
| CN219595896U (en) | Rectifying device | |
| CN208732972U (en) | It is a kind of suitable for cyclohexanol production from backheat energy saver | |
| CN105085176A (en) | Crude glycerin concentration method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |