CN103566613A - Rectification device and process for low-concentration organic solvent aqueous liquor recycling heat pump - Google Patents
Rectification device and process for low-concentration organic solvent aqueous liquor recycling heat pump Download PDFInfo
- Publication number
- CN103566613A CN103566613A CN201210284299.9A CN201210284299A CN103566613A CN 103566613 A CN103566613 A CN 103566613A CN 201210284299 A CN201210284299 A CN 201210284299A CN 103566613 A CN103566613 A CN 103566613A
- Authority
- CN
- China
- Prior art keywords
- stripper
- tower
- heat
- charging aperture
- discharging opening
- 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.)
- Granted
Links
Images
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 the technical field of a chemical separating process and energy saving, and discloses a rectification device and a rectification process for a low-concentration organic solvent aqueous liquor recycling heat pump. The device comprises a feeding preheater (1), a stripping tower (2), a compressor (3), a stripping tower reboiler (4) and a rectifying tower (5) which are connected by a pipeline in sequence. The rectification process comprises the following steps of: adding the aqueous liquor containing a low-concentration organic solvent into the feeding preheater (1) for heating to a bubble point; adding into the stripping tower (2) for carrying out stripping treatment; ventilating vapor extracted from the tower top of the stripping tower (2) into the compressor (3) for compressing, then, ventilating into the stripping tower reboiler (4) as a heat source to carry out heat exchange; carrying out rectification process treatment by using a condensed material from the stripping tower reboiler (4) as a feeding material of the rectifying tower (5), and extracting a product on the tower top of the rectifying tower (5). The rectification device and the rectification process disclosed by the invention are obvious in energy-saving effect.
Description
Technical field
The invention belongs to chemical separation process and field of energy-saving technology, relate to a kind of low concentration aqueous solutions of organic solvent and reclaim heat pump distillation apparatus and technique.
Background technology
In chemical process, often can produce the aqueous solution that contains in a large number low concentration organic solvent, the recovery to the organic solvent in the aqueous solution, adopts rectification process to process at present mostly.But because the concentration of the organic solvent in the aqueous solution is lower, rectifying separation obtains that the required rectifying column number of theoretical plate of purer organic solvent product is high, reflux ratio is high, and energy consumption is large.If adopted first the weak solution concentrate technique of rectifying then, although rectifying column reflux ratio reduces, the first concentrate again energy loss-rate of the whole technique of rectifying is used separately the energy consumption increase to some extent on the contrary of rectification process.
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 trails on a system for separating ethanol and water, International Journal ofEnergy 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 of 2-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, can reduces thermal waste, reduce part energy resource consumption, but above-mentioned technique can not be applied to the larger operating mode of the temperature difference between ubiquitous rectifying tower head tower still.
Summary of the invention
For heat pump techniques being applied to the larger operating mode of the temperature difference between rectifying tower head tower still, the object of this invention is to provide a kind of low concentration organic solvent-aqueous solution and reclaim heat pump distillation apparatus and technique.
Technical scheme of the present invention is as follows:
The invention provides a kind of low concentration aqueous solutions of organic solvent and reclaim heat pump distillation apparatus, this device comprises feed preheater, stripper, compressor, stripper reboiler and rectifying column; Feed preheater, stripper, compressor, stripper reboiler and rectifying column are connected through pipeline successively.
Described feed preheater is provided with feed preheater charging aperture, feed preheater discharging opening, feed preheater heat medium charging aperture and feed preheater heat medium discharging opening, feed preheater heat medium charging aperture is positioned at the side of feed preheater, and feed preheater heat medium discharging opening is positioned at another corresponding side of feed preheater heat medium charging aperture; Feed preheater discharging opening is connected with stripper liquid phase feeding mouth, and feed preheater heat medium charging aperture is connected with discharging opening at the bottom of stripper reboiler tower, and feed preheater heat medium discharging opening is positioned at the bottom of feed preheater charging aperture.
Described stripper is provided with boil again steam inlet, the outlet of stripper tower reactor and the heating steam of stripper tower reactor of stripper liquid phase feeding mouth, stripper overhead extraction mouth, stripper and supplements mouthful, stripper liquid phase feeding mouth is positioned at the side middle and upper part of stripper, the stripper steam inlet of boiling is again positioned at another corresponding side middle and lower part of stripper heat medium charging aperture, stripper overhead extraction mouth is positioned at the top of stripper, and the outlet of stripper tower reactor is positioned at the bottom of stripper; Stripper heat medium charging aperture is connected with feed preheater discharging opening, stripper overhead extraction mouth is connected with compressor charging aperture, the stripper steam inlet of boiling is again connected with stripper reboiler tower top discharging opening, the outlet of stripper tower reactor is connected with stripper reboiler charging aperture, the heating steam of stripper tower reactor supplements mouth and is positioned at stripper tower reactor, is connected with external heat steam supply pipe road.
Described compressor is provided with compressor charging aperture and compressor discharging opening; Compressor charging aperture is connected with stripper overhead extraction mouth, and compressor discharging opening is connected with stripper reboiler heat transferring medium charging aperture.
Described stripper reboiler is provided with stripper reboiler tower top discharging opening, stripper reboiler heat transferring medium charging aperture, stripper reboiler charging aperture, discharging opening and stripper reboiler heat transferring medium discharging opening at the bottom of stripper reboiler tower, stripper reboiler tower top discharging opening is positioned at the top of stripper reboiler, at the bottom of stripper reboiler tower, discharging opening is positioned at the bottom of stripper reboiler, stripper reboiler charging aperture is positioned at the side of stripper reboiler, stripper reboiler heat transferring medium charging aperture and stripper reboiler heat transferring medium discharging opening are positioned at the upper and lower of another corresponding side of stripper reboiler charging aperture, stripper reboiler tower top discharging opening and the stripper steam inlet of boiling is again connected, stripper reboiler heat transferring medium charging aperture is connected with compressor discharging opening, stripper reboiler charging aperture is connected with the outlet of stripper tower reactor, at the bottom of stripper reboiler tower, discharging opening is connected with feed preheater heat medium charging aperture, and stripper reboiler heat transferring medium discharging opening is connected with rectifying column charging aperture.
Described rectifying column is provided with rectifying column tower top extraction mouth, tower bottom of rectifying tower extraction mouth and rectifying column charging aperture, rectifying column tower top extraction mouth is positioned at the top of rectifying column, tower bottom of rectifying tower extraction mouth is positioned at the bottom of rectifying column, and rectifying column charging aperture is positioned at the side of rectifying column; Rectifying column charging aperture is connected with stripper reboiler heat transferring medium discharging opening.
The present invention also provides a kind of low concentration aqueous solutions of organic solvent to reclaim heat-pump rectifying process, and this technique comprises the following steps:
First the aqueous solution that contains low concentration organic solvent is passed into and in feed preheater, be heated to bubble point, pass in stripper and carry and heat up in a steamer processing, then after the material steam of stripper overhead extraction being passed into compressor and compressing, passing into stripper reboiler carries out heat as the thermal source of stripper reboiler and changes, finally, from stripper reboiler condensation material out, as rectifying column charging, carry out rectification process processing, at rectifying column tower top extraction high levels of organic solvents.
Described organic solvent one or more C for dissolving each other with water
1～C
4organic compound.
Described C
1～C
4organic compound be 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.
Described low concentration organic solvent refers to that the mass concentration of organic solvent in water is 3 ~ 20%.
Described feed preheater, stripper reboiler are 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 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 ~ 4.0.
Described rectifying column is selected from sieve-plate tower, a kind of in valve tower or packed tower, and the tower top of rectifying column and the temperature range of tower reactor are 20 ~ 45 ℃.
Compared with the existing technology, tool has the following advantages and beneficial effect in the present invention:
1, the present invention can be widely used in all kinds of organic compound feed separation.
2, the present invention can reduce chemical industry distillation process effectively, particularly adopts the energy resource consumption of the distillation process of heat pump techniques, reduces production costs.
Accompanying drawing explanation
Fig. 1 represents to adopt the heat-pump rectifying process figure of weak solution.
Wherein: 1 is feed preheater, 2 is stripper, 3 is compressor, 4 is stripper reboiler, 5 is rectifying column, 11 is feed preheater charging aperture, 12 is feed preheater discharging opening, 13 is feed preheater heat medium charging aperture, 14 is feed preheater heat medium discharging opening, 21 is stripper liquid phase feeding mouth, 22 is stripper overhead extraction mouth, 23 is the stripper steam inlet of boiling again, 24 is stripper tower reactor discharging opening, 25 is that the heating steam of stripper tower reactor supplements mouth, 31 is compressor charging aperture, 32 is compressor discharging opening, 41 is stripper reboiler tower top discharging opening, 42 is stripper reboiler heat transferring medium charging aperture, 43 is stripper reboiler charging aperture, 44 is discharging opening at the bottom of stripper reboiler tower, 45 is stripper reboiler heat transferring medium discharging opening, 51 is rectifying column tower top extraction mouth, 52 is tower bottom of rectifying tower extraction mouth, 53 is rectifying column charging aperture.
Fig. 2 represents to adopt the conventional distillation artwork of weak solution.
Wherein: 6 is that feed preheater, 7 is that rectifying column, 61 is that feed preheater charging aperture, 62 is that feed preheater discharging opening, 63 is that feed preheater heat medium charging aperture, 64 is that feed preheater heat medium discharging opening, 71 is that rectifying column tower top extraction mouth, 72 is that tower bottom of rectifying tower extraction mouth, 73 is rectifying column charging aperture.
The specific embodiment
Below in conjunction with accompanying drawing illustrated embodiment, the present invention is further illustrated.
In the present invention, unless otherwise defined, all percentage (%) is the mass percent of a certain composition in a certain system, for example, and the mass percent of solute in solution; All " in scopes " include end value, and for example, the mass concentration of organic solvent in water is within the scope of 1%-10%, to comprise 1% and 10%.
Adopt the technological process of the separated rare acetone soln of heat-pump rectifying process as shown in Figure 1.
Concentration is rare acetone soln of 3.5wt%, and flow is 140T/h, and compressor pressure ratios is 3.0, and the rectifying column 7 tower top tower reactor temperature difference are 45 ℃.Feeding temperature is 50 ℃, after feed preheater 1 and stripper reboiler 4 tower bottoms heat exchange to 97 ℃, enters stripper 2 from top, stripping acetone wherein, and guarantee that the content of acetone of tower reactor extraction is less than 100ppm.The acetone water vapours that 90 ℃ of stripper 2 overhead extractions are above, acetone quality content is about 50% left and right, after this steam is heated up by compressor 3 compressions, carry out heat exchange as the thermal source of stripper reboiler 4.Acetone water vapour takes part of the condensate in heat exchange in stripper reboiler 4, and condensation material enters rectifying column 5 and realizes the separated of acetone and water, guarantees that tower top acetone concentration is greater than 98.5wt%, and tower reactor acetone concentration is less than 100ppm.Owing to only depending on the condensation latent heat of acetone water vapour can not meet the demand of stripper reboiler 4, therefore need in stripper 2, pass into part heating steam so that energy to be provided.
Adopt heat-pump rectifying process, guaranteeing that rectifying column 5 overhead product acetone concentration reach 98.5wt.%, tower reactor acetone concentration is less than under 100ppm condition, it is 1.89Gcal/h that stripper 2 need to pass into heating steam heat, rectifying column 5 more boiling hot amount is 0.42Gcal/h, and total consumption of calorie is 2.31Gcal/h.Stripper 2 tower tops are not established condensation, cooler, and the heat exchange amount of rectifying column 5 overhead condensation coolers is 1.35Gcal/h.In addition, the power of compressor 3 is 610KW(0.44GKal/h).
Comparative example 1
Rare acetone soln conventional distillation technological process of 3.5wt% as shown in Figure 2.
Concentration is rare acetone soln of 3.5wt%, and flow is 140T/h, and compressor pressure ratios is 3.0, and the rectifying column 7 tower top tower reactor temperature difference are 45 ℃.Feeding temperature is 50 ℃, through after feed preheater 6 and rectifying column 7 tower bottoms heat exchange to 97 ℃, enters rectifying column 7, and number of actual plates is 50.In reflux ratio, be 3.8 o'clock, rectifying column 7 tower top acetone concentration just can reach 98.5wt%, and rectifying column 7 tower reactor acetone concentration are less than 100ppm.Adopt conventional distillation technique, the rectifying column 7 tower reactors energy consumption of boiling again reaches 4.40Gcal/h, and the cold of the cooling needs of rectifying column 7 overhead condensation is 3.27Gcal/h.
Concentration is the methanol solution of 5.0wt%, and flow is 140T/h, and compressor pressure ratios is 2.0, and the rectifying column 7 tower top tower reactor temperature difference are 40 ℃.By feeding temperature, be 50 ℃, after feed preheater 1 and stripper reboiler 4 tower bottoms heat exchange to 80 ℃, from top, enter stripper 2, stripping methyl alcohol wherein, and guarantee that the methanol content of tower reactor extraction is less than 100ppm.90 ℃ of above, methanol quality content is about 30% left and right methanol-water steam of stripper 2 overhead extraction, after this gas is heated up by compressor 3 compressions, carry out heat exchange as stripper reboiler 4 thermals source.Methanol-water steam takes part of the condensate in heat exchange in stripper reboiler 4, and condensation material enters the separation that rectifying column 5 is realized first alcohol and water, guarantees that tower top methanol concentration is greater than 98.5wt%, and rectifying column 5 tower reactor methanol concentrations are less than 100ppm.Because the condensation latent heat of methanol-water steam can not meet the demand of stripper reboiler 4, so need in stripper 2 tower reactors, pass into part heating steam so that energy to be provided.
Adopt heat-pump rectifying process, guaranteeing that rectifying column 5 overhead product methanol concentrations reach 98.5wt%, tower reactor methanol concentration is less than under 100ppm condition.It is 2.16Gcal/h that stripper 2 need to pass into heating steam heat, and rectifying column 5 more boiling hot amount is 3.35Gcal/h, and total consumption of calorie is 5.51Gcal/h.Stripper 2 tower tops are not established condensation, cooler, and the heat exchange amount of rectifying column 5 overhead condensation coolers is 3.47Gcal/h.In addition, the power of compressor 3 is 705KW(0.61GKa1/h).
Comparative example 2
Concentration is the methanol solution of 5.0wt%, and flow is 140T/h, and compressor pressure ratios is 2.0, and the rectifying column 7 tower top tower reactor temperature difference are 40 ℃.By feeding temperature, be 50 ℃, through after feed preheater 6 and rectifying column 7 tower bottoms heat exchange to 80 ℃, enter rectifying column 7, number of actual plates is 60, and dilute methanol conventional distillation process as shown in Figure 2.In reflux ratio, be 1.6 o'clock, rectifying column 7 tower top methanol concentrations just can reach 98.5wt%, and rectifying column 7 tower reactor methanol concentrations are less than 100ppm.Adopt conventional distillation technique, the rectifying column 7 tower reactors energy consumption of boiling again reaches 11.08Gcal/h, and the cold of the cooling needs of rectifying column 7 overhead condensation is 8.55Gcal/h.
Concentration is the methanol solution of 20.0wt%, and flow is 140T/h, and compressor pressure ratios is 1.5, and the rectifying column 7 tower top tower reactor temperature difference are 30 ℃.By feeding temperature, be 50 ℃, after feed preheater 1 and stripper reboiler 4 tower bottoms heat exchange to 80 ℃, from top, enter stripper 2, stripping methyl alcohol wherein, and guarantee that the methanol content of tower reactor extraction is less than 100ppm.90 ℃ of above, methanol quality content is about 60% left and right methanol-water steam of stripper 2 overhead extraction, after this gas is heated up by compressor 3 compressions, carry out heat exchange as stripper reboiler 4 thermals source.Methanol-water steam takes part of the condensate in heat exchange in stripper reboiler 4, and condensation material enters the separation that rectifying column 5 is realized first alcohol and water, guarantees that tower top methanol concentration is greater than 95wt%, and rectifying column 5 tower reactor methanol concentrations are less than 100ppm.Because the condensation latent heat of methanol-water steam can not meet the demand of stripper reboiler 4, so need in stripper 2 tower reactors, pass into part heating steam so that energy to be provided.
Adopt heat-pump rectifying process, guaranteeing that rectifying column 5 overhead product methanol concentrations reach 95wt%, tower reactor methanol concentration is less than under 100ppm condition.It is 2.54Gcal/h that stripper 2 need to pass into heating steam heat, and rectifying column 5 more boiling hot amount is 6.41Gcal/h, and total consumption of calorie is 8.95Gcal/h.Stripper 2 tower tops are not established condensation, cooler, and the heat exchange amount of rectifying column 5 overhead condensation coolers is 9.68Gcal/h.In addition, the power of compressor 3 is 443KW(0.38Gcal/h).
Comparative example 3
Concentration is the methanol solution of 20.0wt%, and flow is 140T/h, and compressor pressure ratios is 1.5, and the rectifying column 7 tower top tower reactor temperature difference are 30 ℃.By feeding temperature, be 50 ℃, through after feed preheater 6 and rectifying column 7 tower bottoms heat exchange to 80 ℃, enter rectifying column 7, number of actual plates is 45, and dilute methanol conventional distillation process as shown in Figure 2.In reflux ratio, be 2.5 o'clock, rectifying column 7 tower top methanol concentrations can reach 95wt%, and rectifying column 7 tower reactor methanol concentrations are less than 100ppm.Adopt conventional distillation technique, the rectifying column 7 tower reactors energy consumption of boiling again reaches 33.7Gcal/h, and the cold of the cooling needs of rectifying column 7 overhead condensation is 30.6Gcal/h.
As shown in Figure 1, Fig. 1 represents to adopt the heat-pump rectifying process figure of weak solution.
Aqueous solutions of organic solvent reclaims a heat pump distillation apparatus, and this device comprises feed preheater 1, stripper 2, compressor 3, stripper reboiler 4 and rectifying column 5; Feed preheater 1, stripper 2, compressor 3, stripper reboiler 4 and rectifying column 5 are connected through pipeline successively.
Feed preheater 1 is provided with feed preheater charging aperture 11, feed preheater discharging opening 12, feed preheater heat medium charging aperture 13 and feed preheater heat medium discharging opening 14, feed preheater heat medium charging aperture 13 is positioned at the side of feed preheater 1, and feed preheater heat medium discharging opening 14 is positioned at another corresponding side of feed preheater heat medium charging aperture 13; Feed preheater discharging opening 12 is connected with stripper liquid phase feeding mouth 21, and feed preheater heat medium charging aperture 13 is connected with discharging opening 44 at the bottom of stripper reboiler tower, and feed preheater heat medium discharging opening 14 is positioned at the bottom of feed preheater charging aperture 11.
Rectifying column 5 is provided with rectifying column tower top extraction mouth 51, tower bottom of rectifying tower extraction mouth 52 and rectifying column charging aperture 53, rectifying column tower top extraction mouth 51 is positioned at the top of rectifying column 5, tower bottom of rectifying tower extraction mouth 52 is positioned at the bottom of rectifying column 5, and rectifying column charging aperture 53 is positioned at the side of rectifying column 5; Rectifying column charging aperture 53 is connected with stripper reboiler heat transferring medium discharging opening 45.
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. low concentration aqueous solutions of organic solvent reclaims a heat pump distillation apparatus, it is characterized in that: this device comprises feed preheater (1), stripper (2), compressor (3), stripper reboiler (4) and rectifying column (5); Feed preheater (1), stripper (2), compressor (3), stripper reboiler (4) and rectifying column (5) are connected through pipeline successively.
2. low concentration aqueous solutions of organic solvent according to claim 1 reclaims heat pump distillation apparatus, it is characterized in that: described feed preheater (1) is provided with feed preheater charging aperture (11), feed preheater discharging opening (12), feed preheater heat medium charging aperture (13) and feed preheater heat medium discharging opening (14), feed preheater heat medium charging aperture (13) is positioned at the side of feed preheater (1), and feed preheater heat medium discharging opening (14) is positioned at another corresponding side of feed preheater heat medium charging aperture (13); Feed preheater discharging opening (12) is connected with stripper liquid phase feeding mouth (21), feed preheater heat medium charging aperture (13) is connected with discharging opening (44) at the bottom of stripper reboiler tower, and feed preheater heat medium discharging opening (14) is positioned at the bottom of feed preheater charging aperture (11).
3. low concentration aqueous solutions of organic solvent according to claim 1 reclaims heat pump distillation apparatus, it is characterized in that: described stripper (2) is provided with stripper liquid phase feeding mouth (21), stripper overhead extraction mouth (22), the stripper steam inlet (23) of boiling again, stripper tower reactor discharging opening (24) and the heating steam of stripper tower reactor supplement mouthful (25), stripper liquid phase feeding mouth (21) is positioned at the side middle and upper part of stripper (2), the stripper steam inlet (23) of boiling is again positioned at another corresponding side middle and lower part of stripper heat medium charging aperture (21), stripper overhead extraction mouth (22) is positioned at the top of stripper (2), stripper tower reactor discharging opening (24) is positioned at the bottom of stripper (2), stripper heat medium charging aperture (21) is connected with feed preheater discharging opening (12), stripper overhead extraction mouth (22) is connected with compressor charging aperture (31), the stripper steam inlet (23) of boiling is again connected with stripper reboiler tower top discharging opening (41), stripper tower reactor discharging opening (24) is connected with stripper reboiler charging aperture (43), the heating steam of stripper tower reactor supplements mouthful (25) and is positioned at stripper tower reactor, is connected with external heat steam supply pipe road.
4. low concentration aqueous solutions of organic solvent according to claim 1 reclaims heat pump distillation apparatus, it is characterized in that: described compressor (3) is provided with compressor charging aperture (31) and compressor discharging opening (32); Compressor charging aperture (31) is connected with stripper overhead extraction mouth (22), and compressor discharging opening (32) is connected with stripper reboiler heat transferring medium charging aperture (42).
5. low concentration aqueous solutions of organic solvent according to claim 1 reclaims heat pump distillation apparatus, it is characterized in that: described stripper reboiler (4) is provided with stripper reboiler tower top discharging opening (41), stripper reboiler heat transferring medium charging aperture (42), stripper reboiler charging aperture (43), discharging opening at the bottom of stripper reboiler tower (44) and stripper reboiler heat transferring medium discharging opening (45), stripper reboiler tower top discharging opening (41) is positioned at the top of stripper reboiler (4), discharging opening at the bottom of stripper reboiler tower (44) is positioned at the bottom of stripper reboiler (4), stripper reboiler charging aperture (43) is positioned at the side of stripper reboiler (4), stripper reboiler heat transferring medium charging aperture (42) and stripper reboiler heat transferring medium discharging opening (45) are positioned at the upper and lower of another corresponding side of stripper reboiler charging aperture (43), stripper reboiler tower top discharging opening (41) and the stripper steam inlet (23) of boiling is again connected, stripper reboiler heat transferring medium charging aperture (42) is connected with compressor discharging opening (32), stripper reboiler charging aperture (43) is connected with stripper tower reactor discharging opening (24), discharging opening at the bottom of stripper reboiler tower (44) is connected with feed preheater heat medium charging aperture (13), and stripper reboiler heat transferring medium discharging opening (45) is connected with rectifying column charging aperture (53).
6. low concentration aqueous solutions of organic solvent according to claim 1 reclaims heat pump distillation apparatus, it is characterized in that: described rectifying column (5) is provided with rectifying column tower top extraction mouth (51), tower bottom of rectifying tower extraction mouth (52) and rectifying column charging aperture (53), rectifying column tower top extraction mouth (51) is positioned at the top of rectifying column (5), tower bottom of rectifying tower extraction mouth (52) is positioned at the bottom of rectifying column (5), and rectifying column charging aperture (53) is positioned at the side of rectifying column (5); Rectifying column charging aperture (53) is connected with stripper reboiler heat transferring medium discharging opening (45).
7. the low concentration aqueous solutions of organic solvent that the arbitrary described device of claim 1 ~ 6 carries out reclaims heat-pump rectifying process, it is characterized in that: this technique comprises the following steps:
First the aqueous solution that contains low concentration organic solvent is passed in feed preheater (1) and is heated to bubble point, pass in stripper (2) and carry and heat up in a steamer processing, then after the material steam of stripper (2) overhead extraction being passed into compressor (3) and compressing, passing into stripper reboiler (4) carries out heat as the thermal source of stripper reboiler (4) and changes, from stripper reboiler (4) condensation material out as rectifying column (5) charging carry out rectification process processing, at rectifying column (5) overhead extraction high levels of organic solvents.
8. low concentration aqueous solutions of organic solvent according to claim 7 reclaims heat-pump rectifying process, it is characterized in that: described organic solvent one or more C for dissolving each other with water
1～C
4organic compound.
9. low concentration aqueous solutions of organic solvent according to claim 8 reclaims heat-pump rectifying process, it is characterized in that: described C
1～C
4organic compound be 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. low concentration aqueous solutions of organic solvent according to claim 7 reclaims heat-pump rectifying process, it is characterized in that: described low concentration organic solvent refers to that the mass concentration of organic solvent in water is 3 ~ 20%.
11. low concentration aqueous solutions of organic solvent according to claim 7 reclaim heat-pump rectifying process, it is characterized in that: described feed preheater, stripper reboiler are 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. low concentration aqueous solutions of organic solvent according to claim 7 reclaim heat-pump rectifying process, it is characterized in that: described compressor (3) 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 ~ 4.0.
13. low concentration aqueous solutions of organic solvent according to claim 7 reclaim heat-pump rectifying process, it is characterized in that: described rectifying column (5) is selected from sieve-plate tower, a kind of in valve tower or packed tower, the tower top of rectifying column and the temperature range of tower reactor are 20 ~ 45 ℃.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210284299.9A CN103566613B (en) | 2012-08-06 | 2012-08-06 | A kind of low-concentration organic solvent aqueous solution reclaims heat pump distillation apparatus and technique |
| PCT/CN2013/077855 WO2014023136A1 (en) | 2012-08-06 | 2013-06-25 | Low-density organic solvent aqueous solution recycling heat pump assisted distillation device and process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210284299.9A CN103566613B (en) | 2012-08-06 | 2012-08-06 | A kind of low-concentration organic solvent aqueous solution reclaims heat pump distillation apparatus and technique |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103566613A true CN103566613A (en) | 2014-02-12 |
| CN103566613B CN103566613B (en) | 2016-03-30 |
Family
ID=50039857
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210284299.9A Active CN103566613B (en) | 2012-08-06 | 2012-08-06 | A kind of low-concentration organic solvent aqueous solution reclaims heat pump distillation apparatus and technique |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN103566613B (en) |
| WO (1) | WO2014023136A1 (en) |
Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103994603A (en) * | 2014-06-12 | 2014-08-20 | 中国科学院工程热物理研究所 | Chemical heat pump device assisted by ultrasonic radiation |
| CN105348043A (en) * | 2015-11-27 | 2016-02-24 | 河北工业大学 | Separating and recycling method and device for solvent-water mixture containing impurities prone to scale formation |
| CN105435480A (en) * | 2015-12-25 | 2016-03-30 | 佛山德众制药机械有限公司 | Vacuum push-pull alcohol concentration system |
| CN105669412A (en) * | 2016-03-14 | 2016-06-15 | 江苏乐科节能科技股份有限公司 | Acetone solvent recovery heat-pump distillation technology |
| CN106237643A (en) * | 2016-10-08 | 2016-12-21 | 中国科学院理化技术研究所 | MVR heat pump rectification system |
| CN106379952A (en) * | 2015-08-07 | 2017-02-08 | 王树岩 | Apparatus and process for treating ammonia nitrogen wastewater and recycling ammonia |
| CN106957214A (en) * | 2017-04-14 | 2017-07-18 | 江苏乐科节能科技股份有限公司 | Methanol heat-pump distillation system and method |
| CN107158734A (en) * | 2017-06-21 | 2017-09-15 | 河北乐恒化工设备制造有限公司 | The device and its energy-efficient concentrating method of N ethyl piperazidines of energy-efficient concentrate |
| CN110615494A (en) * | 2019-10-31 | 2019-12-27 | 吴嘉 | Post-treatment device and method for complex DMF wastewater after DMF recovery |
| CN111153762A (en) * | 2020-01-22 | 2020-05-15 | 临涣焦化股份有限公司 | Benzene hydrogenation energy-saving efficiency-improving device and use method thereof |
| CN111558231A (en) * | 2020-06-15 | 2020-08-21 | 中国科学院理化技术研究所 | A binary component azeotrope separation system |
| CN111841060A (en) * | 2020-08-31 | 2020-10-30 | 常熟龙飞医药设备科技有限公司 | Organic solvent dehydration device and dehydration method based on heat pump rectification and pervaporation coupling |
| CN112875783A (en) * | 2021-04-14 | 2021-06-01 | 北京中科康仑环境科技研究院有限公司 | System and method for treating wastewater containing volatile substances |
| CN112902686A (en) * | 2021-01-26 | 2021-06-04 | 河北易高生物能源有限公司 | Furfural primary distillation tower steam recycling method |
| CN114396823A (en) * | 2022-01-19 | 2022-04-26 | 连云港石化有限公司 | Waste heat recovery and utilization system of ethylene oxide water solution |
| CN118856667A (en) * | 2024-08-12 | 2024-10-29 | 江苏科诚节能科技有限公司 | Pre-compression heat exchange heat pump energy recovery system and method |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1996011732A1 (en) * | 1993-09-03 | 1996-04-25 | Farmland Industries, Inc. | Apparatus configuration and method of treating process condensate |
| CN101874935A (en) * | 2010-07-05 | 2010-11-03 | 天津大学 | Bottom reboiling type internal heat integrated energy-saving rectification device and method in rectification section |
| CN102451573A (en) * | 2010-11-03 | 2012-05-16 | 中国石油化工股份有限公司 | Rectification method of acetic acid dehydration tower |
| CN101525272B (en) * | 2009-04-07 | 2012-05-30 | 天津大学 | Ethanol distillation dehydration energy saving technique and device |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4539076A (en) * | 1982-09-27 | 1985-09-03 | Swain R L Bibb | Vapor compression distillation system |
| CN101397236B (en) * | 2008-11-19 | 2011-06-15 | 河北工业大学 | Rectification technique for separating ethanol, acetone and butanol fermentation mash |
| CN102430254B (en) * | 2011-09-16 | 2013-09-04 | 徐建涛 | Rectification technology and apparatus of aqueous solution of methanol or ethanol |
| CN102503771B (en) * | 2011-10-12 | 2014-04-16 | 安徽中粮生化燃料酒精有限公司 | Refining system and method of ethanol-containing aqueous solution |
-
2012
- 2012-08-06 CN CN201210284299.9A patent/CN103566613B/en active Active
-
2013
- 2013-06-25 WO PCT/CN2013/077855 patent/WO2014023136A1/en active Application Filing
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1996011732A1 (en) * | 1993-09-03 | 1996-04-25 | Farmland Industries, Inc. | Apparatus configuration and method of treating process condensate |
| CN101525272B (en) * | 2009-04-07 | 2012-05-30 | 天津大学 | Ethanol distillation dehydration energy saving technique and device |
| CN101874935A (en) * | 2010-07-05 | 2010-11-03 | 天津大学 | Bottom reboiling type internal heat integrated energy-saving rectification device and method in rectification section |
| CN102451573A (en) * | 2010-11-03 | 2012-05-16 | 中国石油化工股份有限公司 | Rectification method of acetic acid dehydration tower |
Non-Patent Citations (1)
| Title |
|---|
| 朱平等: "分割式热泵精馏的研究及其分割点的确定", 《西安交通大学学报》, vol. 32, no. 1, 31 January 1998 (1998-01-31), pages 93 - 96 * |
Cited By (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103994603A (en) * | 2014-06-12 | 2014-08-20 | 中国科学院工程热物理研究所 | Chemical heat pump device assisted by ultrasonic radiation |
| CN106379952A (en) * | 2015-08-07 | 2017-02-08 | 王树岩 | Apparatus and process for treating ammonia nitrogen wastewater and recycling ammonia |
| CN105348043A (en) * | 2015-11-27 | 2016-02-24 | 河北工业大学 | Separating and recycling method and device for solvent-water mixture containing impurities prone to scale formation |
| CN105435480A (en) * | 2015-12-25 | 2016-03-30 | 佛山德众制药机械有限公司 | Vacuum push-pull alcohol concentration system |
| CN105435480B (en) * | 2015-12-25 | 2017-07-11 | 佛山德众制药机械有限公司 | Vacuum recommends alcohol concentration systems |
| CN105669412A (en) * | 2016-03-14 | 2016-06-15 | 江苏乐科节能科技股份有限公司 | Acetone solvent recovery heat-pump distillation technology |
| CN106237643A (en) * | 2016-10-08 | 2016-12-21 | 中国科学院理化技术研究所 | MVR heat pump rectification system |
| CN106237643B (en) * | 2016-10-08 | 2018-06-26 | 中国科学院理化技术研究所 | MVR heat pump rectification system |
| CN106957214A (en) * | 2017-04-14 | 2017-07-18 | 江苏乐科节能科技股份有限公司 | Methanol heat-pump distillation system and method |
| CN107158734A (en) * | 2017-06-21 | 2017-09-15 | 河北乐恒化工设备制造有限公司 | The device and its energy-efficient concentrating method of N ethyl piperazidines of energy-efficient concentrate |
| CN110615494A (en) * | 2019-10-31 | 2019-12-27 | 吴嘉 | Post-treatment device and method for complex DMF wastewater after DMF recovery |
| CN110615494B (en) * | 2019-10-31 | 2023-11-10 | 格琳嘉(杭州)科技发展有限公司 | Post-treatment device and method for complex DMF wastewater after DMF recovery |
| CN111153762A (en) * | 2020-01-22 | 2020-05-15 | 临涣焦化股份有限公司 | Benzene hydrogenation energy-saving efficiency-improving device and use method thereof |
| CN111153762B (en) * | 2020-01-22 | 2023-12-29 | 临涣焦化股份有限公司 | Benzene hydrogenation energy-saving efficiency improving device and application method thereof |
| CN111558231A (en) * | 2020-06-15 | 2020-08-21 | 中国科学院理化技术研究所 | A binary component azeotrope separation system |
| CN111841060A (en) * | 2020-08-31 | 2020-10-30 | 常熟龙飞医药设备科技有限公司 | Organic solvent dehydration device and dehydration method based on heat pump rectification and pervaporation coupling |
| CN112902686A (en) * | 2021-01-26 | 2021-06-04 | 河北易高生物能源有限公司 | Furfural primary distillation tower steam recycling method |
| CN112875783A (en) * | 2021-04-14 | 2021-06-01 | 北京中科康仑环境科技研究院有限公司 | System and method for treating wastewater containing volatile substances |
| CN114396823A (en) * | 2022-01-19 | 2022-04-26 | 连云港石化有限公司 | Waste heat recovery and utilization system of ethylene oxide water solution |
| CN118856667A (en) * | 2024-08-12 | 2024-10-29 | 江苏科诚节能科技有限公司 | Pre-compression heat exchange heat pump energy recovery system and method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103566613B (en) | 2016-03-30 |
| WO2014023136A1 (en) | 2014-02-13 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103566613B (en) | A kind of low-concentration organic solvent aqueous solution reclaims heat pump distillation apparatus and technique | |
| CN104817481B (en) | Technological method for recovering DMSO from DMSO aqueous solution | |
| CN102875329B (en) | A kind of heat pump distillation is separated technique and the device of primary isoamyl alcohol isomers | |
| CN203710716U (en) | Device for improving recycling rate of alcohol ketone components in refining process of cyclohexanone | |
| CN103566612B (en) | A kind of compression heat pump rectifier unit and technique | |
| CN103788026A (en) | Method of purifying propylene epoxide | |
| CN110404285A (en) | Four-column distillation and membrane separation integrated system and method for distilling ethanol | |
| CN101139249A (en) | An energy-saving distillation process for recovering low-concentration alcohol | |
| CN102225889B (en) | Method for preparing dimethyl ether by dehydration of methanol | |
| CN102895791A (en) | Novel methanol three-tower rectification apparatus and technology | |
| CN109876485A (en) | Acetic acid recovery is from backheat rectifier unit and method | |
| CN110105216A (en) | A kind of method and device from backheat rectifying | |
| CN107137949B (en) | Extraction and rectification partition plate tower device and method for dehydrating low-concentration isopropanol solution | |
| CN106316791B (en) | Alcohol based on double thick and double smart towers is for device and method | |
| CN101982450B (en) | Method for recovering butanol-butyl acetate from waste acid water generated during antibiotic production through reduced pressure distillation | |
| CN103086854B (en) | Method and device for reducing methanol content in formaldehyde process by silver method | |
| CN203677978U (en) | Vapor-compression type alcohol recovery tower | |
| CN106746118A (en) | A kind of system and method for utilization heat recovery from sewage alcohol ketone | |
| CN205307847U (en) | Device that continuous extrinsic cycle extraction rectification and interior condensation layering combine | |
| CN111807959A (en) | Energy-saving process and process equipment for n-propyl acetate | |
| CN218553132U (en) | Device for recovering ethanol by single-effect evaporation coupling supergravity rectification | |
| CN110711400A (en) | Energy-saving caprolactam production system and method by evaporating caprolactam water solution | |
| CN221905796U (en) | A glycerol purification device capable of effectively removing methanol and water | |
| CN222517753U (en) | Device for recovering multi-component organic solvent mother liquor through hypergravity reduced pressure rectification | |
| CN220597096U (en) | Recovery treatment device for waste water containing n-butyl acetate |
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 |