CN102532506B - Heat-integrated concentration and vaporization separating method - Google Patents
Heat-integrated concentration and vaporization separating method Download PDFInfo
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- CN102532506B CN102532506B CN2012100428142A CN201210042814A CN102532506B CN 102532506 B CN102532506 B CN 102532506B CN 2012100428142 A CN2012100428142 A CN 2012100428142A CN 201210042814 A CN201210042814 A CN 201210042814A CN 102532506 B CN102532506 B CN 102532506B
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- vapour
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- heat exchanger
- interchanger
- heat
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- 238000000034 method Methods 0.000 title claims abstract description 37
- 238000009834 vaporization Methods 0.000 title abstract description 11
- 230000008016 vaporization Effects 0.000 title abstract description 11
- 229920005989 resin Polymers 0.000 claims abstract description 22
- 239000011347 resin Substances 0.000 claims abstract description 22
- 239000002904 solvent Substances 0.000 claims abstract description 22
- 239000000463 material Substances 0.000 claims abstract description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 12
- 238000001816 cooling Methods 0.000 claims abstract description 8
- 239000012141 concentrate Substances 0.000 claims abstract description 4
- 238000004458 analytical method Methods 0.000 claims description 22
- 229920000515 polycarbonate Polymers 0.000 claims description 19
- 239000004417 polycarbonate Substances 0.000 claims description 19
- YMWUJEATGCHHMB-UHFFFAOYSA-N Dichloromethane Chemical compound ClCCl YMWUJEATGCHHMB-UHFFFAOYSA-N 0.000 claims description 16
- 238000004891 communication Methods 0.000 claims description 16
- 238000010438 heat treatment Methods 0.000 claims description 5
- 238000007701 flash-distillation Methods 0.000 claims description 4
- 230000004907 flux Effects 0.000 claims description 2
- 239000007791 liquid phase Substances 0.000 claims description 2
- 230000000694 effects Effects 0.000 abstract description 5
- 238000005516 engineering process Methods 0.000 abstract description 3
- 238000009833 condensation Methods 0.000 abstract description 2
- 230000005494 condensation Effects 0.000 abstract description 2
- 238000001704 evaporation Methods 0.000 abstract description 2
- 239000000126 substance Substances 0.000 abstract description 2
- 230000008020 evaporation Effects 0.000 abstract 1
- 239000003795 chemical substances by application Substances 0.000 description 7
- 239000002245 particle Substances 0.000 description 5
- 238000001556 precipitation Methods 0.000 description 4
- 238000005266 casting Methods 0.000 description 3
- 229920005668 polycarbonate resin Polymers 0.000 description 3
- 239000004431 polycarbonate resin Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 238000001035 drying Methods 0.000 description 2
- 238000005469 granulation Methods 0.000 description 2
- 230000003179 granulation Effects 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000012716 precipitator Substances 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000007766 curtain coating Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 230000021715 photosynthesis, light harvesting Effects 0.000 description 1
- 238000010008 shearing Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
Images
Classifications
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
Abstract
The invention relates to a heat-integrated concentration and vaporization separating method, and belongs to the technical field of chemical condensation and vaporization separating equipment. The heat-integrated concentration and vaporization separating method comprises the following steps of: firstly, separating materials behind a vaporization separating tube into a product and tail gas by a separator; secondly, making the product enter a sequential processing process, and making the tail gas enter a second heat exchanger to heat a resin solution before entering a ejector so as to realize primary recycle of the energy of the tail, where the tail gas after the primary heat exchange has a relatively high temperature because the tail gas contains a large amount of water vapor, solvent and the like; thirdly, making the tail gas enter a first heat exchanger in front of a flash tank to heat the materials so as to perform flash evaporation on the materials in the flash tank and concentrate the materials to improve the concentration of the solution for performing secondary recycle of the energy; and finally, making the tail gas enter a third heat exchanger, and cooling the tail gas. The heat-integrated concentration and vaporization separating method is reliable in principle and simple and convenient in process; the device used in the heat-integrated concentration and vaporization separating method is simple in structure, flexible in operation, good in separating effect, mature in technology and process, and can save energy and improve the efficiency.
Description
Technical field:
The invention belongs to Chemical concentration vapour desorption device technical field, relate to a kind of hot integrated concentration vapour analysis method, be applied to the occasion of separating of polycarbonate and solvent.
Background technology:
Polycarbonate (PC) is the technological process that energy expenditure was maximum during PC produced with separated from solvent, selects suitable separation scheme and separating device, and is significant to the energy expenditure and the steady running that reduce complete assembly.The separation method of PC and solvent has the precipitator method, elutriation method, vapour to analyse method, casting method and heating power method etc. in industrial production at present.The precipitator method are to utilize precipitation agent that PC is precipitated out from solution, precipitation agent is added in the PC solution under violent stirring, PC namely is powdery or granular separating out, it must be dissolving resin and reasonable mutual solubility is arranged with solvent not that this method requires precipitation agent, and with separating than being easier to of solvent, the precipitation agent of polycarbonate comprises alcohols, ester class, ketone and arene etc.; Elutriation method is to utilize the elutriation tower that polycarbonate solution is sprayed in the hot water flow, solvent and hot water azeotropic and vaporize, polycarbonate resin then is cotton-shaped and is suspended in the hot water, the cotton-shaped resin that is suspended in the hot water enters water strainer through separator, spray cold water makes the resin cooling in the water strainer, resin is dried in loft drier after moving into centrifuge dewatering after the cooling, again through the extruding granulator granulation; It is to utilize steam and polycarbonate resin solution directly to carry out heat exchange that vapour is analysed method, solvent is heated vaporization and polycarbonate is separated out, utilize injector to make polycarbonate resin solution atomizing and the quick heat exchange of high-temperature steam, the solvent vaporization of being heated, the solvent of vaporization is condensed into liquid state through snubber, water cooler and flow to storage tank by separator, powdered resin is the further drying solvent and the moisture that remove participation then, send granulation in the extruding granulator; Casting method is that polycarbonate solution curtain coating on casting machine is become thickness is the thin slice of 2 millimeter, blow down solvent with warm air, the thin slice that obtains is cut into particle again, also resin solution directly can be made the film of different thickness, and solvent reclaims with condensation method or absorption method; The heating power method be will be concentrated resin solution on the twin-roll plasticator, by the shearing force between cylinder and heat effect, water and solvent are volatilized gradually, solvent reclaims after cooling, and resin is loose block through plasticating into scale, and this block resin is after dry approximately half an hour about 90 ℃, use again pulverizer broken, get powder-material, drying extrudes into particle.Adopt vapour to analyse the more of method in the existing industrial production, the higher cooling process of directly carrying out of exhaust temperature after vapour is analysed but existing vapour is analysed in the method not only will consume mass energy, and wasted the energy that tail gas itself carries, if the material concentration that sprays is not high, also be that meeting increases the consumption of steam and steam consumption is increased.Generally speaking, existing isolation technique ubiquity that device structure is complicated, and the separating technology process is more, and energy dissipation is many, consume large, and the outstanding shortcoming such as automatic control level is low.
Summary of the invention:
The object of the invention is to overcome the shortcoming that prior art exists, seek to design and a kind ofly the vapour of polycarbonate and solvent effective separation can be analysed technical scheme, adopt the concentrated vapour of hot integration mode to analyse technique, realize energy-conservation and effect that enhance productivity.It is to utilize steam and resin solution directly to carry out heat exchange in injector that vapour is analysed process, solvent is heated vaporization and makes polycarbonate separate out the formation particle, then the particle that forms is analysed pipe through vapour and is continued heating, further dried particles, evaporating solvent, energy in this process is except being used for the loss of dried material and equipment, and most energy has all entered in the middle of the tail vapour, so that vapour is analysed the later tail stripping temperature of pipe is very high; Because the viscosity of resin solution is very high; so to need in the past to be heated to certain temperature just passable entering injector; so can utilize these tail vapour that the front resin is heated easily; effectively utilize the energy of tail vapour; utilize also can reducing for processing the needed energy of tail vapour of tail vapour energy, just can play the conserve energy protection of the environment with the effect of increasing economic efficiency.Entering the quantity of steam that the resin concentration of injector analyses process to vapour has a great impact, when the resin solution concentration ratio is lower, solvent is larger, so in injector, need the amount of steam to increase, therefore improve the concentration that enters the front resin solution of injector and can save the quantity of steam that enters injector; So the tail vapour that utilizes vapour to analyse the pipe back heats before resin solution is entered injector, then carries out flash distillation, evaporates some solvents, is conducive to the utilization of tail vapour energy.
To achieve these goals, the inventive method is carried out in the vapour analysis apparatus, first vapour is analysed the material of pipe back and in a separator, isolate product and tail vapour, product introduction subsequent disposal operation, tail vapour enters the second interchanger, heat entering injector resin solution before, recycle in this first time of carrying out tail vapour energy, owing to contain a large amount of water vapors and solvent etc., also higher through the exhaust temperature after the heat exchange, so tail vapour enters the First Heat Exchanger of flash tank front again material is heated, so that material in the back in the flash tank flash distillation concentrate and improve strength of solution, what carry out is that tail vapour energy is recycled for the second time herein, and last tail vapour enters the 3rd interchanger and carries out cooling process.
The vapour analysis apparatus agent structure that the present invention uses comprises that First Heat Exchanger, flash tank, the second interchanger, injector, vapour analyses pipe, separator and the 3rd interchanger; The bottom of flash tank is communicated with the second heat exchanger tube, the top of flash tank and First Heat Exchanger pipeline communication, and the front end of First Heat Exchanger docks with the 3rd interchanger communication type; The output terminal of the second interchanger and First Heat Exchanger pipeline communication, another output terminal of the second interchanger and injector dock pipeline communication; The formula of ganging up is shaped with vapour and analyses pipe in the connecting pipeline of injector and separator, and dock with the second interchanger communication type at the top of separator; Be shaped with inlet mouth and air outlet on the 3rd interchanger; Be shaped with inlet mouth on the First Heat Exchanger; The place, top of flash tank is shaped with inlet mouth; The place, bottom of separator is shaped with discharge port.
The present invention compared with prior art, its principle is safe and reliable, simple process, the apparatus structure of use is simple, operation is used flexibly, good separating effect, technical maturity can utilize tail gas energy, saves energy, raises the efficiency, and increases economic benefit.
Description of drawings:
Fig. 1 is process structure principle schematic of the present invention, and its agent set comprises that First Heat Exchanger 1, flash tank 2, the second interchanger 3, injector 4, vapour analyses pipe 5, separator 6 and the 3rd interchanger 7.
Embodiment:
Also be described further by reference to the accompanying drawings below by embodiment.
Embodiment:
Present embodiment carries out in vapour analysis apparatus shown in Figure 1, first vapour is analysed the material of pipe 5 back and in separator 6, isolate product and tail gas, product introduction subsequent disposal operation, tail gas enters the second interchanger 3, heat entering injector 4 resin solution before, recycle in this first time of carrying out tail gas energy; Also higher through the exhaust temperature after the heat exchange, 1 pair of material of First Heat Exchanger that tail gas enters flash tank 2 fronts again heats, so that material in the back in the flash tank 2 flash distillation concentrate and improve strength of solution, what carry out is that tail gas energy is recycled for the second time herein, and last tail gas enters the 3rd interchanger 7 and carries out cooling process.
The vapour analysis apparatus agent structure that present embodiment uses comprises that First Heat Exchanger 1, flash tank 2, the second interchanger 3, injector 4, vapour analyses pipe 5, separator 6 and the 3rd interchanger 7; The bottom of flash tank 2 and the second interchanger 3 pipeline communications, the top of flash tank 2 and First Heat Exchanger 1 pipeline communication, the front end of First Heat Exchanger 1 docks with the 3rd interchanger 7 communication types; The output terminal of the second interchanger 3 and First Heat Exchanger 1 pipeline communication, another output terminal of the second interchanger 3 and injector 4 dock pipeline communications; The formula of ganging up is shaped with vapour and analyses pipe 5 in the connecting pipeline of injector 4 and separator 6, and dock with the second interchanger 3 communication types at the top of separator 6; Be shaped with inlet mouth and two air outlets on the 3rd interchanger 7; Be shaped with inlet mouth on the First Heat Exchanger 1; The place, top of flash tank 2 is shaped with inlet mouth; The place, bottom of separator 6 is shaped with the air outlet.
The liquid that present embodiment is selected is the resin solution that is dissolved with polycarbonate in the methylene dichloride, polycarbonate wherein: the mass ratio of methylene dichloride=0.12: 0.88, temperature is 25 ℃, total flux is 24361kg/h, heating reaches 80 ℃ later through tail vapour by First Heat Exchanger 1, needing energy is 496.6kW, then enter flash tank 2 and carry out flash concentration, liquid phase quality 20371kg/h after concentrated, quality is than polycarbonate: methylene dichloride=0.144: 0.856, temperature is at 40 ℃, it is 126.5kW that material after concentrated is heated to 60 ℃ of needs energy by tail vapour, then carry out vapour and analyse, the tail stripping temperature after vapour is analysed is 110 ℃, and tail vapour is steam and methylene dichloride, by calculating as can be known, analysing the front later tail stripping temperature of the second interchanger 3 heat exchange through vapour is 90 ℃, is 88.9 ℃ through the temperature behind the First Heat Exchanger 1, and it recycles tail gas 623.1kW energy.
Claims (1)
1. hot integrated concentration vapour analysis method, it is characterized in that first vapour being analysed the material of managing the back and in a separator, isolate product and tail vapour, product introduction subsequent disposal operation, tail vapour enters the second interchanger, heat entering injector resin solution before, recycle in this first time of carrying out tail vapour energy, owing to contain a large amount of water vapors and solvent, also higher through the exhaust temperature after the heat exchange, so tail vapour enters the First Heat Exchanger of flash tank front again material is heated, so that material in the back in the flash tank flash distillation concentrate and improve strength of solution, what carry out is that tail vapour energy is recycled for the second time herein, and last tail vapour enters the 3rd interchanger and carries out cooling process; The structure of employed vapour analysis apparatus comprises that First Heat Exchanger, flash tank, the second interchanger, injector, vapour analyses pipe, separator and the 3rd interchanger; The bottom of flash tank is communicated with the second heat exchanger tube, the top of flash tank and First Heat Exchanger pipeline communication, and the front end of First Heat Exchanger docks with the 3rd interchanger communication type; The output terminal of the second interchanger and First Heat Exchanger pipeline communication, another output terminal of the second interchanger and injector dock pipeline communication; The formula of ganging up is shaped with vapour and analyses pipe in the connecting pipeline of injector and separator, and dock with the second interchanger communication type at the top of separator; Be shaped with inlet mouth and air outlet on the 3rd interchanger; Be shaped with inlet mouth on the First Heat Exchanger; The place, top of flash tank is shaped with inlet mouth; The place, bottom of separator is shaped with discharge port; Select the resin solution that is dissolved with polycarbonate in the methylene dichloride, polycarbonate wherein: the mass ratio=0.12:0.88 of methylene dichloride, temperature is 25 ℃, total flux is 24361kg/h, heating reaches 80 ℃ later through tail vapour by First Heat Exchanger, needing energy is 496.6kW, then enter flash tank and carry out flash concentration, liquid phase quality 20371kg/h after concentrated, quality is than polycarbonate: methylene dichloride=0.144:0.856, and temperature is at 40 ℃, it is 126.5kW that material after concentrated is heated to 60 ℃ of needs energy by tail vapour, then carry out vapour and analyse, the tail stripping temperature after vapour is analysed is 110 ℃, and tail vapour is steam and methylene dichloride, by calculating as can be known, analysing the front later tail stripping temperature of the second interchanger heat exchange through vapour is 90 ℃, is 88.9 ℃ through the temperature behind the First Heat Exchanger, and it recycles tail gas 623.1kW energy.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012100428142A CN102532506B (en) | 2012-02-24 | 2012-02-24 | Heat-integrated concentration and vaporization separating method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012100428142A CN102532506B (en) | 2012-02-24 | 2012-02-24 | Heat-integrated concentration and vaporization separating method |
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| Publication Number | Publication Date |
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| CN102532506A CN102532506A (en) | 2012-07-04 |
| CN102532506B true CN102532506B (en) | 2013-04-24 |
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| CN2012100428142A Expired - Fee Related CN102532506B (en) | 2012-02-24 | 2012-02-24 | Heat-integrated concentration and vaporization separating method |
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| CN102964584B (en) * | 2012-11-14 | 2014-12-31 | 万华化学集团股份有限公司 | Purification method of crude polycarbonate solution |
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| CA786154A (en) * | 1968-05-28 | B. Carel Alfred | Vapor phase chromatography system | |
| CN1153180A (en) * | 1995-11-03 | 1997-07-02 | 通用电气公司 | Vapor precipitation of polymers from solvent polymer blends by azeotropic spray drying |
| CN100534580C (en) * | 2007-09-28 | 2009-09-02 | 天津大学 | Gas-chromatography separating device and technique for azeotrope separation |
| CN201246981Y (en) * | 2008-07-14 | 2009-05-27 | 广州赛唯热工设备有限公司 | Flash evaporation crystallization tank sheet type waste heat recovery device |
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