CN105669362A - Trichloromethane solvent recovery heat pump rectification process - Google Patents
Trichloromethane solvent recovery heat pump rectification process Download PDFInfo
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- CN105669362A CN105669362A CN201610139722.4A CN201610139722A CN105669362A CN 105669362 A CN105669362 A CN 105669362A CN 201610139722 A CN201610139722 A CN 201610139722A CN 105669362 A CN105669362 A CN 105669362A
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- tower
- chloroform
- steam
- solvent recovery
- reboiler
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/38—Separation; Purification; Stabilisation; Use of additives
- C07C17/383—Separation; Purification; Stabilisation; Use of additives by distillation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
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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
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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
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a trichloromethane solvent recovery heat pump rectification process, and belongs to the field of heat pump rectification.A fed material (10) is heated through a preheater and then enters a rectification tower (1), the main separation task is completed in the rectification tower, trichloromethane steam (5) with the concentration of 85%-99.99% is extracted from the tower top, the trichloromethane steam (5) is pressurized and heated through a steam compressor, and compressed trichloromethane steam (6) enters the hot side of a reboiler (3), exchanges heat with a tower kettle liquid phase and then is condensed into a liquid phase; after the raw material (10) is preheated by the liquid phase via the hot side of the preheater (5), one part serves as a tower top discharged material (7), and the other part serves as tower top reflux liquid (8); the raw material at a tower kettle outlet is divided into two paths, one path is evaporated into a gas phase through the cold side of the reboiler (3) and enters the tower bottom, and the other path serves as a tower bottom heavy component discharged material (9); the operating pressure of the rectification is 50 kPa-300 kPa, the reflux ratio is 1.5-6, and the compression ratio of the steam compressor is 1.5-6.By means of the trichloromethane solvent recovery heat pump rectification process, energy consumption in traditional production is lowered.
Description
Technical field
The invention belongs to heat pump distillation field, relate to the new technology of a kind of chloroform solvent heat pump distillation.
Background technology
Chloroform is organic synthesis raw material, is mainly used to produce freon (F-21, F-22, F-23), dyestuff and medicine, medically, is commonly used for anesthetis. Can be used as antibiotic, spice, oils and fats, resin, the solvent of rubber and extractant. The fire-fighting liquid that may be manufactured without freezing is mixed with carbon tetrachloride. Be additionally operable to the propellant powder of aerosol, corn fumigant and calibration temperature titer. Industrial products, generally added with a small amount of ethanol, make the phosgene of generation generate nontoxic diethyl carbonate with ethanol effect. Use and can add washing after a small amount of concentrated sulphuric acid jolting before industrial goods, dry through calcium chloride or potassium carbonate, chloroform without ethanol.
Chloroform is generally by-product when producing chloridising production dichloromethane, and the method for rectification can be adopted to realize purifying, and the distance pulled open due to respective boiling point is relatively larger, it is possible to carry out separating-purifying conveniently by common fractionating technology. This production technology overhead vapours pressure is far below kettle material temperature, and therefore tower reactor must use a large amount of raw steam preheating, and energy consumption is too high.
Summary of the invention
It is an object of the invention to provide a kind of chloroform solvent recovery heat-pump rectifying process, reduce the energy consumption in Conventional process.
A kind of chloroform solvent recovery heat-pump rectifying process, it is characterised in that: distillation system is made up of rectifying column, vapour compression machine, reboiler, preheater; The preheated device of charging heats up and enters in rectifying column, main separation task completes in rectifying column, the chloroform steam of overhead extraction 85%-99.99% concentration, chloroform steam heats up through vapour compression machine boosting, and the chloroform steam after compression enters the hot side of reboiler, after tower reactor liquid phase heat exchange, being condensed into liquid phase, the hot side of the preheated device of this liquid phase, after preheating material, a part is as tower top discharging, and a part is as overhead reflux; Tower reactor outlet is divided into two-way, and a road is evaporated to gas phase through the cold side of reboiler and enters at the bottom of tower, and a road is as heavy constituent discharging at the bottom of tower. The application in chloroform soln reclaims of described pump rectification method, it is characterised in that: described rectifying column operation pressure is 50kPa 300kPa, and reflux ratio is 0.5 6;Described vapour compression machine, compression ratio is 26.
Described chloroform solvent recovery heat-pump rectifying process, it is characterised in that: described rectifying column is plate column or packed tower.
Described chloroform solvent recovery heat-pump rectifying process, it is characterised in that: described reboiler is plate type heat exchanger, or forced circulation heat exchange.
Described chloroform solvent recovery heat-pump rectifying process, it is characterised in that: described vapour compression machine is roots-type or centrifugal or double-screw type.
It is an advantage of the current invention that: utilize heat pump distillation as chloroform solvent recovery mode, compared with tradition rectification mode, it is possible to save the consumption of a large amount of condensed water and steam, operating cost can be substantially reduced. Meet the requirement of industry energy conservation consumption reduction.
Accompanying drawing explanation
Fig. 1-heat pump technology flow chart;
Fig. 2-original distillation process figure;
Fig. 3-present invention and tradition distillation system Operation cost comparison figure;
Number in the figure title: 1-rectifying column tower body; 2-compressor; 3-reboiler; 4-preheater; 5-tower top chloroform steam; Chloroform steam after 6-pressure; 7-tower top discharging; 8-overhead reflux; 9-tower reactor discharging; 10-charging; 11-condenser; 12-condensed water; 13-steam.
It is embodied as example
Embodiment 1
Below in conjunction with accompanying drawing to illustrating:
Certain unit existing needs to consist of chloroform 88%, and the raw material of tetrachloromethane 11% and other heavy constituents separates, it is desirable to chloroform concentration is more than 99.99%, and treating capacity is 5t/h.
A kind of chloroform solvent recovery heat-pump rectifying process, is mainly made up of rectifying column 1, compressor 2, reboiler 3 and preheater 4.
Described rectifying column 1 adopts packed tower, main separation task completes in tower, the chloroform steam 5 of overhead extraction 99.99% concentration, chloroform steam heats up through vapour compression machine 2 boosting, chloroform steam 6 after compression is as the thermal source of reboiler 3, after reboiler heat exchange, chloroform steam is condensed into chloroform soln, after this liquid phase preheated device 4 preheating material, a part is as recycling design discharging 7, concentration is 99.99%, and a part is as the backflow 8 of rectifying column, tower reactor extraction heavy constituent 10.
It is 50kPa that described rectifying column 1 operates pressure, and tower top chloroform steam 5 temperature is 41 DEG C, and reflux ratio is 3.
Described vapour compression machine compression ratio is 6, and Compressor Discharge Pressure is 300kPa, and temperature is 98 DEG C.
Described preheater is feed preheater, and raw material 10 is preheated to close to bubble point by chloroform steam condensate.
Described reboiler is tower top compressed steam 6 and tower reactor liquid phase heat exchange place, and bottom temperature is 89 DEG C.
With tradition distillation system accompanying drawing 2 compared with, adopt heat pump rectification system can steam saving 4.6t/h, recirculated water 384t/h(32 DEG C 38 DEG C), increase power consumption 602kW. Calculate with current price, 160 yuan/t of steam, 0.2 yuan/t of recirculated water, the electricity charge 0.8 yuan/degree, the two year Operation cost comparison such as Fig. 3 (the annual operation time presses 8000h and calculates):
From figure 3, it can be seen that for the chloroform solvent recovery unit of 5.3t/h charging, the more traditional rectification of operating cost adopting heat pump distillation annual saves more than 130 ten thousand yuan, has greatly saved the investment of enterprise, has reduced energy consumption.
Embodiment 2
Certain enterprise, using chloroform as extractant, adopts the mode of rectification by chloroform solvent recovery, it is desirable to tower top chloroform concentration is higher than 90%, and treating capacity is 8t/h, and wherein Determination of Trichloro Methane is 50%.
A kind of chloroform solvent recovery heat-pump rectifying process, is mainly made up of rectifying column 1, compressor 2, reboiler 3 and preheater 4. Described rectifying column 1 adopts packed tower, main separation task completes in tower, the chloroform steam 5 of overhead extraction 95% concentration, chloroform steam heats up through vapour compression machine 2 boosting, chloroform steam 6 after compression is as the thermal source of reboiler 3, after reboiler heat exchange, chloroform steam is condensed into chloroform soln, after this liquid phase preheated device 4 preheating material, a part is as recycling design discharging 7, concentration is 95%, and a part is as the backflow 8 of rectifying column, tower reactor extraction heavy constituent 10.
It is 300kPa that described rectifying column 1 operates pressure, and reflux ratio is 6, and tower top temperature is 98 DEG C.
Described vapour compression machine 2 compression ratio is 2, and Compressor Discharge Pressure is 600kPa, and temperature is 128 DEG C.
Described preheater is feed preheater, and raw material 10 is preheated to close to bubble point by chloroform steam condensate.
Described reboiler is tower top compressed steam 6 and tower reactor liquid phase heat exchange place, and bottom temperature is 120 DEG C.
Adopt chloroform heat-pump rectifying process, 2.4t/h steam consumption can be reduced, it is possible to decrease the operating cost of nearly 40%.
Embodiment 3
Certain factory produces certain product with chloroform for solvent, it is necessary to reclaiming chloroform, its treating capacity is 2t/h, and wherein Determination of Trichloro Methane is 60%, it is desirable to tower top chloroform concentration is more than 80%.
A kind of chloroform solvent recovery heat-pump rectifying process, is mainly made up of rectifying column 1, compressor 2, reboiler 3 and preheater 4. Described rectifying column 1 adopts packed tower, main separation task completes in tower, the chloroform steam 5 of overhead extraction 85% concentration, chloroform steam heats up through vapour compression machine 2 boosting, chloroform steam 6 after compression is as the thermal source of reboiler 3, after reboiler heat exchange, chloroform steam is condensed into chloroform soln, after this liquid phase preheated device 4 preheating material, a part is as recycling design discharging 7, concentration is 85%, and a part is as the backflow 8 of rectifying column, tower reactor extraction heavy constituent 10.
It is 100kPa that described rectifying column 1 operates pressure, and reflux ratio is 0.5, and tower top temperature is 60 DEG C.
Described vapour compression machine 2 compression ratio is 3, and Compressor Discharge Pressure is 300kPa, and temperature is 98 DEG C.
Described preheater is feed preheater, and raw material 10 is preheated to close to bubble point by chloroform steam condensate.
Described reboiler is tower top compressed steam 6 and tower reactor liquid phase heat exchange place, and bottom temperature is 90 DEG C.
Adopt heat-pump rectifying process, this operating mode steam saving 0.8t/h can be made, greatly reduce operating cost.
Claims (4)
1. a chloroform solvent recovery heat-pump rectifying process, it is characterised in that: distillation system is made up of rectifying column (1), vapour compression machine (2), reboiler (3), preheater (4); The preheated device of charging (10) heats up and enters in rectifying column (1), main separation task completes in rectifying column, the chloroform steam (5) of overhead extraction 85%-99.99% concentration, chloroform steam (5) heats up through vapour compression machine boosting, chloroform steam (6) after compression enters the hot side of reboiler (3), after tower reactor liquid phase heat exchange, it is condensed into liquid phase, this liquid phase preheated device (5) hot side, after preheating material (10), a part is as tower top discharging (7), and a part is as overhead reflux (8);Tower reactor outlet is divided into two-way, and a road is evaporated to gas phase through the cold side of reboiler (3) and enters at the bottom of tower, and a road is as heavy constituent discharging (9) at the bottom of tower; Described rectifying column operation pressure is 50kPa 300kPa, and reflux ratio is 0.5 6; Described vapour compression machine, compression ratio is 26.
2. chloroform solvent recovery heat-pump rectifying process according to claim 1, it is characterised in that: described rectifying column (1) is plate column or packed tower.
3. chloroform solvent recovery heat-pump rectifying process according to claim 1, it is characterised in that: described reboiler (3) is plate type heat exchanger, or forced circulation heat exchange.
4. chloroform solvent recovery heat-pump rectifying process according to claim 1, it is characterised in that: described vapour compression machine (2) is roots-type or centrifugal or double-screw type.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610139722.4A CN105669362A (en) | 2016-03-14 | 2016-03-14 | Trichloromethane solvent recovery heat pump rectification process |
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| CN201610139722.4A CN105669362A (en) | 2016-03-14 | 2016-03-14 | Trichloromethane solvent recovery heat pump rectification process |
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| CN105669362A true CN105669362A (en) | 2016-06-15 |
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| CN201610139722.4A Pending CN105669362A (en) | 2016-03-14 | 2016-03-14 | Trichloromethane solvent recovery heat pump rectification process |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN107137949A (en) * | 2017-07-11 | 2017-09-08 | 河北工业大学 | A kind of extracting rectifying partitioned column device and method of low concentration aqueous isopropanol dehydration |
| CN108079610A (en) * | 2018-01-15 | 2018-05-29 | 苏州欧拉透平机械有限公司 | Energy-saving methanol rectifying system and its rectificating method |
| CN109665940A (en) * | 2019-01-07 | 2019-04-23 | 天津乐科节能科技有限公司 | Methanol is from backheat distillation system and application |
| CN110449096A (en) * | 2018-05-08 | 2019-11-15 | 中国石化工程建设有限公司 | A kind of process and aromatic device low-grade utility system improving aromatic device low-grade utility efficiency |
| CN110551003A (en) * | 2018-05-31 | 2019-12-10 | 杨祖杰 | System and process for preparing sodium methoxide by heat pump compression circulation double towers |
| CN112827207A (en) * | 2021-02-25 | 2021-05-25 | 浙江宸轩透平机制造有限公司 | Mechanical chemical medium vapor recompression rectification device and method |
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| US5252187A (en) * | 1991-07-25 | 1993-10-12 | Toyo Engineering Corporation | Method of recovering solvent from mother liquor containing non-volatile matters by heat pump system |
| EP2746246A1 (en) * | 2012-12-20 | 2014-06-25 | Solvay SA | Process for the manufacture of ethylene dichloride (EDC), and process for the manufacture of vinyl chloride monomer (VCM) and of polyvinyl chloride (PVC) |
| WO2015033935A1 (en) * | 2013-09-06 | 2015-03-12 | 株式会社ダイセル | Method and plant for using recompressed vapor |
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2016
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Patent Citations (3)
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|---|---|---|---|---|
| US5252187A (en) * | 1991-07-25 | 1993-10-12 | Toyo Engineering Corporation | Method of recovering solvent from mother liquor containing non-volatile matters by heat pump system |
| EP2746246A1 (en) * | 2012-12-20 | 2014-06-25 | Solvay SA | Process for the manufacture of ethylene dichloride (EDC), and process for the manufacture of vinyl chloride monomer (VCM) and of polyvinyl chloride (PVC) |
| WO2015033935A1 (en) * | 2013-09-06 | 2015-03-12 | 株式会社ダイセル | Method and plant for using recompressed vapor |
Non-Patent Citations (1)
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| 许维秀等: "化工节能中的热泵精馏工艺流程分析", 《节能》 * |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN107137949A (en) * | 2017-07-11 | 2017-09-08 | 河北工业大学 | A kind of extracting rectifying partitioned column device and method of low concentration aqueous isopropanol dehydration |
| CN107137949B (en) * | 2017-07-11 | 2020-03-13 | 河北工业大学 | Extraction and rectification partition plate tower device and method for dehydrating low-concentration isopropanol solution |
| CN108079610A (en) * | 2018-01-15 | 2018-05-29 | 苏州欧拉透平机械有限公司 | Energy-saving methanol rectifying system and its rectificating method |
| CN108079610B (en) * | 2018-01-15 | 2024-02-23 | 苏州欧拉透平机械有限公司 | Energy-saving methanol rectifying device and rectifying method thereof |
| CN110449096A (en) * | 2018-05-08 | 2019-11-15 | 中国石化工程建设有限公司 | A kind of process and aromatic device low-grade utility system improving aromatic device low-grade utility efficiency |
| CN110551003A (en) * | 2018-05-31 | 2019-12-10 | 杨祖杰 | System and process for preparing sodium methoxide by heat pump compression circulation double towers |
| CN109665940A (en) * | 2019-01-07 | 2019-04-23 | 天津乐科节能科技有限公司 | Methanol is from backheat distillation system and application |
| CN112827207A (en) * | 2021-02-25 | 2021-05-25 | 浙江宸轩透平机制造有限公司 | Mechanical chemical medium vapor recompression rectification device and method |
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Application publication date: 20160615 |