CN109665940A - Methanol is from backheat distillation system and application - Google Patents
Methanol is from backheat distillation system and application Download PDFInfo
- Publication number
- CN109665940A CN109665940A CN201910010763.7A CN201910010763A CN109665940A CN 109665940 A CN109665940 A CN 109665940A CN 201910010763 A CN201910010763 A CN 201910010763A CN 109665940 A CN109665940 A CN 109665940A
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- China
- Prior art keywords
- compressor
- cycle fluid
- tower reactor
- distillation system
- heat
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- 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.)
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 108
- 238000004821 distillation Methods 0.000 title claims abstract description 25
- 239000012530 fluid Substances 0.000 claims abstract description 47
- 239000003507 refrigerant Substances 0.000 claims abstract description 29
- 230000008676 import Effects 0.000 claims abstract description 16
- 238000001816 cooling Methods 0.000 claims abstract description 11
- 230000006835 compression Effects 0.000 claims abstract description 8
- 238000007906 compression Methods 0.000 claims abstract description 8
- 238000011084 recovery Methods 0.000 claims abstract description 7
- 238000010438 heat treatment Methods 0.000 claims abstract description 5
- 238000000034 method Methods 0.000 claims description 10
- 239000007791 liquid phase Substances 0.000 claims description 7
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 2
- 239000007792 gaseous phase Substances 0.000 claims description 2
- MSSNHSVIGIHOJA-UHFFFAOYSA-N pentafluoropropane Chemical compound FC(F)CC(F)(F)F MSSNHSVIGIHOJA-UHFFFAOYSA-N 0.000 claims description 2
- QGHDLJAZIIFENW-UHFFFAOYSA-N 4-[1,1,1,3,3,3-hexafluoro-2-(4-hydroxy-3-prop-2-enylphenyl)propan-2-yl]-2-prop-2-enylphenol Chemical group C1=C(CC=C)C(O)=CC=C1C(C(F)(F)F)(C(F)(F)F)C1=CC=C(O)C(CC=C)=C1 QGHDLJAZIIFENW-UHFFFAOYSA-N 0.000 claims 1
- 150000001335 aliphatic alkanes Chemical class 0.000 claims 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 8
- 238000005516 engineering process Methods 0.000 abstract description 2
- 239000000243 solution Substances 0.000 description 11
- 239000012071 phase Substances 0.000 description 10
- 239000007788 liquid Substances 0.000 description 9
- 238000009833 condensation Methods 0.000 description 7
- 230000005494 condensation Effects 0.000 description 7
- 239000007864 aqueous solution Substances 0.000 description 6
- 239000007789 gas Substances 0.000 description 6
- 238000004064 recycling Methods 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000000498 cooling water Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000002360 explosive Substances 0.000 description 2
- NSGXIBWMJZWTPY-UHFFFAOYSA-N 1,1,1,3,3,3-hexafluoropropane Chemical compound FC(F)(F)CC(F)(F)F NSGXIBWMJZWTPY-UHFFFAOYSA-N 0.000 description 1
- JRHNUZCXXOTJCA-UHFFFAOYSA-N 1-fluoropropane Chemical compound CCCF JRHNUZCXXOTJCA-UHFFFAOYSA-N 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 210000003205 muscle Anatomy 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 239000012453 solvate Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a kind of Methanol Recoveries from backheat distillation system, it include: rectifying column, overhead condenser and tower reactor reboiler, it is characterized in that, a compressor is equipped between the refrigerant exit of the overhead condenser and the tower reactor reboiler heat source import, circulation has cycle fluid in the compressor, the cycle fluid enters tower reactor reboiler heat source import after compressor compresses heat and exchanges heat with tower bottoms, cycle fluid after cooling is flowed out from tower reactor reboiler thermal source outlet, into overhead condenser refrigerant inlet and exchange heat with overhead vapours, it is returned in compressor after heating.Compared with traditional technology, use electrical energy drive compressor that cycle fluid is carried out compression heating as the heat source of tower reactor from backheat distillation system using of the invention, the use of a large amount of steam and recirculated water has been saved, 25% operation operating cost can be saved under same operating condition every year.
Description
Technical field
The invention belongs to solvent recovery technical fields, and in particular to a kind of methanol is from backheat distillation system and application.
Background technique
Methanol has many advantages, such as that aqueous solution freezing point is low, can dissolve each other completely with water, low corrosion, cheap, ample supply and prompt delivery, is
A kind of important organic solvent.But methanol has strong toxicity to human body, inflammable, steam can form explosive mix with air
Object, chance open fire, high thermal energy cause combustion explosion, therefore in order to protect environment and save production cost, need the first in recycling design
Alcohol.
For the method that the recycling of methanol solvate generallys use rectifying, but this method energy consumption is higher, and recyclable heat is very
Few, most heat can not be recycled by recirculated cooling water directly cooling.
Summary of the invention
It is an object of the invention to overcome the deficiencies of the prior art and provide a kind of energy-efficient methanol from backheat distillation system.
It is a further object to provide a kind of above-mentioned applications from backheat distillation system in recycling methanol.
The present invention is achieved by the following technical solutions:
A kind of methanol is from backheat distillation system, comprising: rectifying column, overhead condenser and tower reactor reboiler, wherein the tower
It pushes up and is equipped with a compressor between the refrigerant exit and the tower reactor reboiler heat source import of condenser, there is circulation in the compressor
Cycle fluid, the cycle fluid enter tower reactor reboiler heat source import after compressor compresses heat and exchange heat with tower bottoms,
Cycle fluid after cooling is flowed out from tower reactor reboiler thermal source outlet, into the refrigerant inlet and and overhead vapours of overhead condenser
It exchanges heat, is returned in compressor after heating.
In the above-mentioned technical solutions, the cycle fluid is R245 (pentafluoropropane), R123 (trifluorobichloroethane) or six
Fluoro-propane.
In the above-mentioned technical solutions, it is set between the thermal source outlet of the tower reactor reboiler and the refrigerant inlet of overhead condenser
There is a heat exchanger, for further cooling down the cycle fluid.
In the above-mentioned technical solutions, a flash distillation is equipped between the cycle fluid outlet and tower top refrigerant inlet of the heat exchanger
Tank, the gaseous phase outlet of the flash tank are connected with the inlet duct of the compressor, and the liquid-phase outlet and tower top of flash tank are cold
The refrigerant inlet pipeline of condenser is connected.
In the above-mentioned technical solutions, the compressor is lobed rotor compressor, double-screw compressor or centrifugal compressor.
In the above-mentioned technical solutions, the pressure ratio of the compressor is 1.1~4.
In the above-mentioned technical solutions, the compressor carries out compression to heat process being single stage compress or multistage to cycle fluid
Compression.
Application of the above-mentioned methanol from backheat distillation system in Methanol Recovery.
In the above-mentioned technical solutions, feeding temperature is 40~80 DEG C, and bottom temperature is 70~100 DEG C, methanol in charging
Concentration is 50~90%.
The advantages and benefits of the present invention are:
1. present invention recovery tower top heat by the way of compressing indirectly heats tower reactor, i.e., compressor does not connect directly
Process stream, compressor compresses cycle fluid are touched, cycle fluid exchanges heat with tower bottoms and overhead vapours respectively again, thus real
The recycling of existing heat.Methanol is inflammable and explosive liquid, and the material containing methanol not directly enters compressor, reduces and fire wind
Danger.
2. in technical solution of the present invention, the cycle fluid in compressor is environmental protection, nonflammable substance is carrying out equipment
The firebreak of compressor and device need not be considered when arrangement, (between the process unit and combustible gas compression machine of production methanol
Away from should be 9m), the space in process units area is greatly saved.
3. using electrical energy drive compressor by circulation industrial from backheat distillation system using of the invention compared with traditional technology
Matter carries out heat source of the compression heating as tower reactor, has saved the use of a large amount of steam and recirculated water, can save every year under same operating condition
Save about 25% operation operating cost.
Detailed description of the invention
Fig. 1 is the general flow chart of the distillation system of the embodiment of the present invention 1；
Wherein, 1 is rectifying column, and 2 be overhead condenser, and 3 be compressor, and 4 be tower reactor reboiler, and 5 be heat exchanger, and 6 be sudden strain of a muscle
Steaming pot.
Specific embodiment
In order to enable those skilled in the art to better understand the solution of the present invention, in the following with reference to the drawings and specific embodiments into
One step illustrates technical solution of the present invention.
Embodiment 1
A kind of methanol is from backheat distillation system, comprising: rectifying column, overhead condenser and tower reactor reboiler.Temperature is 40 DEG C,
The methanol aqueous solution that methanol content is 50% enters rectifying column, which is atmospheric tower, and overhead vapours enters overhead condenser condensation,
Condenser temperature is 55 DEG C, and refrigerant uses cycle fluid, the refrigerant exit of overhead condenser and tower reactor reboiler heat source import it
Between be equipped with a double-screw compressor, the inlet and outlet pressure of compressor is respectively 470kPa and 1550kPa, pressure ratio 3.3, the pressure
Circulation has cycle fluid in contracting machine, which is R245, and the cycle fluid enters tower reactor after compressor compresses heat
Reboiler heat source import, and the condensation (bottom temperature be 100 DEG C) in tower reactor reboiler, the cycle fluid after heat release from tower reactor again
The outflow of device thermal source outlet is boiled, a heat exchanger is equipped between the thermal source outlet of tower reactor reboiler and the refrigerant inlet of overhead condenser, is used
In further cooling down the cycle fluid using recirculated water.Cycle fluid enters a flash tank after heat exchanger outflow, is flashed
The gas-liquid two-phase for being 470kPa at pressure, wherein gas phase returns to the entrance of compressor, liquid phase return to the refrigerant of overhead condenser into
Mouthful, and in overhead condenser absorb overhead vapours heat and evaporate.
In the present invention, cycle fluid evaporation endothermic in overhead condenser, after compressor boost heats tower reactor again
Heat release is condensed in boiling device, tower top heat recovery to tower reactor is used, overhead vapours (methanol) is directly compressed with compressor to tower reactor
The scheme for making heat source is compared, and while realizing that heat recovery recycles, safety is higher, and it is contaminated to reduce overhead product
Risk ensure that the purity of product.
Embodiment 2
A kind of methanol is from backheat distillation system, comprising: rectifying column, overhead condenser and tower reactor reboiler.Temperature is 50 DEG C,
The methanol aqueous solution that methanol content is 90% enters rectifying column, which is atmospheric tower, and overhead vapours enters overhead condenser condensation,
Condenser temperature is 55 DEG C, and refrigerant uses cycle fluid, the refrigerant exit of overhead condenser and tower reactor reboiler heat source import it
Between be equipped with a double-screw compressor, the inlet and outlet pressure of compressor is respectively 470kPa and 1550kPa, pressure ratio 3.3, the pressure
Circulation has cycle fluid in contracting machine, which is R245, and the cycle fluid enters tower reactor after compressor compresses heat
Reboiler heat source import, and the condensation (bottom temperature be 100 DEG C) in tower reactor reboiler, the cycle fluid after heat release from tower reactor again
The outflow of device thermal source outlet is boiled, a heat exchanger is equipped between the thermal source outlet of tower reactor reboiler and the refrigerant inlet of overhead condenser, is used
In further cooling down the cycle fluid using recirculated water.Cycle fluid enters a flash tank after heat exchanger outflow, is flashed
The gas-liquid two-phase for being 470kPa at pressure, wherein gas phase returns to the entrance of compressor, liquid phase return to the refrigerant of overhead condenser into
Mouthful, and in overhead condenser absorb overhead vapours heat and evaporate.
Embodiment 3
A kind of methanol is from backheat distillation system, comprising: rectifying column, overhead condenser and tower reactor reboiler.Temperature is 60 DEG C,
The methanol aqueous solution that methanol content is 90% enters rectifying column, which is atmospheric tower, and overhead vapours enters overhead condenser condensation,
Condenser temperature is 55 DEG C, and a Roots is equipped between the refrigerant exit and tower reactor reboiler heat source import of overhead condenser and is compressed
Machine, the inlet and outlet pressure of compressor are respectively 470kPa and 750kPa, pressure ratio 1.6, and circulation has circulation industrial in the compressor
Matter, the cycle fluid are R245, and the cycle fluid enters tower reactor reboiler heat source import after compressor compresses heat, with tower
Kettle liquid heat exchange, the cycle fluid after cooling flow out (bottom temperature is 71 DEG C), tower reactor reboiler from tower reactor reboiler thermal source outlet
Thermal source outlet and overhead condenser refrigerant inlet between be equipped with a heat exchanger, for using recirculated water further to cool down the circulation
Working medium.Cycle fluid enters a flash tank after heat exchanger outflow, is flashed to the gas-liquid two-phase that pressure is 470kPa, wherein
Gas phase returns to the entrance of compressor, and liquid phase returns to the refrigerant inlet of overhead condenser and exchanges heat with overhead vapours.
In the present embodiment, it is the energy consumption for reducing compressor and rectifying column, reduces the temperature of tower reactor, make tower reactor Produced Liquid
In still have a large amount of methanol, a new rectifying column can be set again and further recycled.The present embodiment is further compared with Example 2
Reduce operating cost (operating cost comprising new rectifying column).
Embodiment 4
A kind of methanol is from backheat distillation system, comprising: rectifying column, overhead condenser and tower reactor reboiler.Temperature is 70 DEG C,
The methanol aqueous solution that methanol content is 80% enters rectifying column, which is atmospheric tower, and overhead vapours enters overhead condenser condensation,
Condenser temperature is 55 DEG C, and a pair of screw compression is equipped between the refrigerant exit and tower reactor reboiler heat source import of overhead condenser
Machine, the inlet and outlet pressure of compressor are respectively 300kPa and 1150kPa, pressure ratio 3.8, and circulation has circulation industrial in the compressor
Matter, the cycle fluid are R123, and the cycle fluid enters tower reactor reboiler heat source import after compressor compresses heat, with tower
Kettle liquid heat exchange, the cycle fluid after cooling are flowed out from tower reactor reboiler thermal source outlet, the thermal source outlet and tower top of tower reactor reboiler
A heat exchanger is equipped between the refrigerant inlet of condenser, for using recirculated water further to cool down the cycle fluid.Cycle fluid from
Enter a flash tank after heat exchanger outflow, the gas-liquid two-phase that pressure is 300kPa is flashed in flash tank, wherein gas phase returns to
The entrance of compressor, liquid phase return to the refrigerant inlet of overhead condenser and exchange heat with overhead vapours.
Embodiment 5
A kind of methanol is from backheat distillation system, comprising: rectifying column, overhead condenser and tower reactor reboiler.Temperature is 80 DEG C,
The methanol aqueous solution that methanol content is 60% enters rectifying column, which is atmospheric tower, and overhead vapours enters overhead condenser condensation,
Condenser temperature is 55 DEG C, and a Roots is equipped between the refrigerant exit and tower reactor reboiler heat source import of overhead condenser and is compressed
Machine, the inlet and outlet pressure of compressor are respectively 800kPa and 900kPa, pressure ratio 1.1, and circulation has circulation industrial in the compressor
Matter, the cycle fluid are hexafluoropropane, and the cycle fluid enters tower reactor reboiler heat source import after compressor compresses heat,
Exchange heat with tower bottoms, cycle fluid after cooling is flowed out from tower reactor reboiler thermal source outlet, the thermal source outlet of tower reactor reboiler with
A heat exchanger is equipped between the refrigerant inlet of overhead condenser, for using recirculated water further to cool down the cycle fluid.Circulation industrial
Matter enters a flash tank after heat exchanger outflow, is flashed to the gas-liquid two-phase that pressure is 800kPa, wherein gas phase returns to pressure
The entrance of contracting machine, liquid phase return to the refrigerant inlet of overhead condenser and exchange heat with overhead vapours.
The comparison of operating cost needed for method of the method for traditional rectifying with the embodiment of the present invention 1 see the table below.
(according to device location concrete condition, according to 150 yuan/ton of steam price, 0.7 yuan of electricity price/degree, cooling water price
0.2 yuan/m3, annual to be calculated by 8000 hours runing times)
By comparison it is found that recycling methanol from backheat distillation system using of the invention, 25% production operation can be saved
Expense meets environmental requirement, not only safe but also reliable.
Illustrative description has been done to the present invention above, it should explanation, the case where not departing from core of the invention
Under, any simple deformation, modification or other skilled in the art can not spend the equivalent replacement of creative work equal
Fall into protection scope of the present invention.
Claims (9)
1. a kind of methanol is from backheat distillation system, comprising: rectifying column, overhead condenser and tower reactor reboiler, which is characterized in that institute
It states and is equipped with compressor between the refrigerant exit of overhead condenser and the tower reactor reboiler heat source import, circulation in the compressor
There is cycle fluid, the cycle fluid enters tower reactor reboiler heat source import for changing with tower bottoms after compressor compresses heat
Heat, the cycle fluid after cooling are flowed out from tower reactor reboiler thermal source outlet, and the refrigerant inlet into overhead condenser is used for and tower
Top steam exchanges heat, and returns in compressor after heating.
2. distillation system according to claim 1, the cycle fluid is pentafluoropropane, trifluorobichloroethane or hexafluoro third
Alkane.
3. distillation system according to claim 1 to 2, the thermal source outlet and overhead condenser of the tower reactor reboiler
Refrigerant inlet between be equipped with a heat exchanger, for further cooling down the cycle fluid.
4. distillation system according to claim 1 to 3, the cycle fluid outlet of the heat exchanger and tower top refrigerant into
A flash tank is equipped between mouthful, the gaseous phase outlet of the flash tank is connected with the inlet duct of the compressor, flash tank
Liquid-phase outlet is connected with the refrigerant inlet pipeline of overhead condenser.
5. distillation system according to claim 1 to 4, the compressor be lobed rotor compressor, double-screw compressor or
Centrifugal compressor.
6. -5 any distillation system according to claim 1, the pressure ratio of the compressor is 1.1~4.
7. -6 any distillation system according to claim 1, the compressor carries out compression to cycle fluid and heats process
For single stage compress or multi-stage compression.
8. application of any distillation system in Methanol Recovery according to claim 1~7.
9. application as claimed in claim 8, feeding temperature is 40~80 DEG C, and bottom temperature is 70~100 DEG C, first in charging
Determining alcohol is 50~90%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910010763.7A CN109665940A (en) | 2019-01-07 | 2019-01-07 | Methanol is from backheat distillation system and application |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910010763.7A CN109665940A (en) | 2019-01-07 | 2019-01-07 | Methanol is from backheat distillation system and application |
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| Publication Number | Publication Date |
|---|---|
| CN109665940A true CN109665940A (en) | 2019-04-23 |
Family
ID=66150477
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910010763.7A Pending CN109665940A (en) | 2019-01-07 | 2019-01-07 | Methanol is from backheat distillation system and application |
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| Country | Link |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110115852A (en) * | 2019-05-07 | 2019-08-13 | 中国科学院理化技术研究所 | Organic solvent rectifying recyclable device |
| CN111302922A (en) * | 2020-03-27 | 2020-06-19 | 北京诺维新材科技有限公司 | Rectification separation method and rectification system |
| CN111389039A (en) * | 2020-03-18 | 2020-07-10 | 谢海刚 | Rectification heat energy closed circulation energy-saving system |
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| CN106075947A (en) * | 2016-06-03 | 2016-11-09 | 天津大学 | Methanol four tower double-effect heat pump energy-saving equipment and method |
| 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 |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110115852A (en) * | 2019-05-07 | 2019-08-13 | 中国科学院理化技术研究所 | Organic solvent rectifying recyclable device |
| CN110115852B (en) * | 2019-05-07 | 2022-04-19 | 中国科学院理化技术研究所 | Organic solvent rectification recovery device |
| CN111389039A (en) * | 2020-03-18 | 2020-07-10 | 谢海刚 | Rectification heat energy closed circulation energy-saving system |
| CN111389039B (en) * | 2020-03-18 | 2023-07-07 | 谢海刚 | Energy-saving system for rectifying heat energy closed circulation |
| CN111302922A (en) * | 2020-03-27 | 2020-06-19 | 北京诺维新材科技有限公司 | Rectification separation method and rectification system |
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Application publication date: 20190423 |