CN110963890B - Refining method of gaseous methanol - Google Patents
Refining method of gaseous methanol Download PDFInfo
- Publication number
- CN110963890B CN110963890B CN201911398747.6A CN201911398747A CN110963890B CN 110963890 B CN110963890 B CN 110963890B CN 201911398747 A CN201911398747 A CN 201911398747A CN 110963890 B CN110963890 B CN 110963890B
- Authority
- CN
- China
- Prior art keywords
- methanol
- tower
- gas
- compressor
- recovery
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 646
- 238000007670 refining Methods 0.000 title claims abstract description 42
- 238000000034 method Methods 0.000 title claims abstract description 31
- 238000011084 recovery Methods 0.000 claims abstract description 86
- 239000012535 impurity Substances 0.000 claims abstract description 19
- 239000007788 liquid Substances 0.000 claims description 26
- 230000008569 process Effects 0.000 claims description 7
- 239000002699 waste material Substances 0.000 claims description 7
- 239000011259 mixed solution Substances 0.000 claims description 6
- 239000012071 phase Substances 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 239000000243 solution Substances 0.000 claims description 3
- 238000009835 boiling Methods 0.000 claims description 2
- 239000007791 liquid phase Substances 0.000 claims description 2
- 230000006835 compression Effects 0.000 abstract description 10
- 238000007906 compression Methods 0.000 abstract description 10
- 230000008901 benefit Effects 0.000 abstract description 5
- 239000007789 gas Substances 0.000 description 47
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 15
- 239000002351 wastewater Substances 0.000 description 8
- WQDUMFSSJAZKTM-UHFFFAOYSA-N Sodium methoxide Chemical compound [Na+].[O-]C WQDUMFSSJAZKTM-UHFFFAOYSA-N 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- 239000000047 product Substances 0.000 description 4
- 238000010992 reflux Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 238000011144 upstream manufacturing Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- GBMDVOWEEQVZKZ-UHFFFAOYSA-N methanol;hydrate Chemical compound O.OC GBMDVOWEEQVZKZ-UHFFFAOYSA-N 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 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
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention provides a refining method of gaseous methanol, which uses a double-tower heat pump rectifying system consisting of a methanol tower, a recovery tower and a heat pump to purify and separate crude methanol gas containing impurities, a compressor compresses the refined methanol gas, and heat is supplied to the methanol tower and the recovery tower after the grade of methanol steam is improved. By reasonably using the compressor and setting reasonable dividing points and reasonably matching the operating pressure of the two towers, the invention realizes the double functions of heat pump heat supply and methanol gas pressurization and has the advantages of low compression ratio of the compressor, low heat consumption of methanol refining and the like.
Description
Technical Field
The invention belongs to the field of methanol refining, and particularly relates to a refining method of gaseous methanol.
Background
Methanol is an extremely important basic organic chemical raw material, can directly participate in the reaction to synthesize downstream chemicals, and can also be used as a stripping agent for separating or refining the chemicals. When methanol is used as a stripping agent, gaseous methanol strips impurities from the liquid chemicals, and the impurities are transferred from the liquid chemicals to the gaseous methanol. The methanol is not consumed, so that a matched methanol refining system is needed at the downstream of the stripping system, crude methanol gas discharged from the stripping tower is separated, refined and recovered, impurities are removed, and the methanol gas is returned to the stripping system for recycling after reaching qualified purity. Since this process is a cyclic process, power must be introduced into the cycle to ensure stable operation of the cycle, i.e., pressurizing the methanol is required.
For example, methanol is used as stripping agent in the production process of sodium methoxide, and gas-phase methanol continuously strips out water as a byproduct of the synthesis reaction from a reaction system, so that the smooth progress of the reaction is ensured; the stripped crude methanol gas is refined and pressurized and then returned to the upstream for recycling. The stripping methanol in the sodium methoxide production process has large dosage and high purity, so that a large amount of energy is consumed in the methanol refining process, and the production cost of sodium methoxide is greatly increased. The methanol refining generally adopts a rectification method, if common rectification is adopted, qualified methanol in a liquid state is required to be produced, then the pressure is increased by a pump, finally high-pressure gas can be obtained by heating and vaporization, and a large amount of heat is consumed in the rectification and vaporization processes; if common heat pump rectification is adopted, a compressor with high compression ratio is needed, and the construction cost and the operation cost are increased as well.
Disclosure of Invention
In view of the above, the invention aims to provide a refining method of gaseous methanol, which can greatly reduce the heat input of a methanol refining system and the compression ratio of a compressor while ensuring the acquisition of high-pressure gaseous refined methanol, thereby reducing the energy consumption of methanol refining, reducing the production cost, saving energy and having good economic and social benefits.
In order to achieve the above purpose, the technical scheme of the invention is realized as follows:
a refining method of gaseous methanol uses a double-tower rectifying system consisting of a methanol tower, a recovery tower and a compressor to purify and separate crude methanol gas containing impurities, and the high-temperature gas obtained by compression of the compressor supplies heat to the methanol tower and the recovery tower.
Further, the method comprises the following steps:
the double-tower rectifying system comprises a methanol tower reboiler and a recovery tower reboiler, wherein the methanol tower reboiler is communicated with the methanol tower to form a loop, and the recovery tower reboiler is communicated with the recovery tower to form a loop.
The crude methanol gas is sent to a methanol tower for separation, mixed liquid of methanol and impurities is extracted from the tower bottom of the methanol tower, and refined methanol gas is extracted from the tower top of the methanol tower;
the refined methanol gas extracted from the top of the methanol tower is pressurized by a compressor, the steam grade is improved to obtain high-grade gas, the high-grade gas supplies heat to a reboiler of the methanol tower and a reboiler of a recovery tower, and a stream of pressurized gaseous methanol is extracted from an outlet of the compressor to be taken as refined methanol product to be sent out of a methanol refining system;
and (3) delivering the mixed solution of the methanol and the impurities extracted from the tower bottom of the methanol tower to a recovery tower for further separation, condensing the gas extracted from the tower top of the recovery tower to obtain methanol-rich solution, extracting qualified waste liquid containing the impurities from the tower bottom of the recovery tower, and delivering the qualified waste liquid to a methanol refining system.
Further, the heat required by the methanol tower reboiler and the recovery tower reboiler is provided by high-grade gas at the outlet of the compressor.
Further, the operating pressure of the recovery column is lower than the operating pressure of the methanol column, and at this operating pressure, the temperature of the bottoms of the recovery column is lower than the saturation temperature of the compressor outlet gas. The condition meets the requirement of heat transfer temperature difference, so that the high-pressure high-temperature gas at the outlet of the compressor can smoothly supply heat to the recovery tower reboiler.
Further, the recovery tower is provided with a tower top condenser, the tower top gas of the recovery tower is condensed to obtain a methanol-rich liquid, and after the methanol-rich liquid is pressurized by a pump, a part of the methanol-rich liquid is used as a return flow to the tower top of the recovery tower, and a part of the methanol-rich liquid is used as a tower top product of the recovery tower to be sent to the methanol tower.
The gas at the top of the recovery tower is pumped back to the methanol tower in a liquid phase mode after being condensed, and is not directly returned to the methanol tower in a gas phase mode, so that the operating pressure of the recovery tower can be lower than that of the methanol tower, and the temperature of the tower bottom of the recovery tower can be reduced.
Further, the temperature of the bottom liquid of the methanol tower is lower than the saturation temperature of the gas at the outlet of the compressor.
The composition of the kettle liquid of the methanol tower meets the condition that the temperature of the kettle liquid of the methanol tower is lower than the saturation temperature of gas at the outlet of the compressor under the composition, and meets the requirement of heat transfer temperature difference at the moment, so that the high-pressure high-temperature gas at the outlet of the compressor can supply heat to the reboiler of the methanol tower.
Further, the crude methanol feed is a gas phase feed, the refined methanol discharge is a gas phase discharge, and the refined methanol discharge pressure is higher than the crude methanol feed pressure.
Furthermore, the methanol tower reboiler and the recovery tower reboiler can form a series heating passage or a parallel heating passage, and all condensate discharged by the methanol tower reboiler and the recovery tower reboiler is used as a return flow to be returned to the top of the methanol tower.
Furthermore, the serial heat supply passage is that the high-grade gas at the outlet of the compressor enters the methanol tower reboiler and the recovery tower reboiler in series to supply heat, and the parallel heat supply passage is that the high-grade gas at the outlet of the compressor enters the methanol tower reboiler and the recovery tower reboiler in parallel to supply heat.
Further, the boiling point of the impurity is higher than that of methanol under the same pressure, and the impurity does not form a low azeotrope with methanol. Such as water, etc.
Further, the bubble point temperature of the bottom liquid of the recovery tower is 5-30 ℃ lower than the dew point temperature of the gas at the outlet of the compressor. The design of the temperature difference can ensure that the high-pressure high-temperature gas at the outlet of the compressor can supply heat to the reboiler of the recovery tower. Preferably, the bubble point temperature of the bottoms liquid of the recovery tower is 15 ℃ or 20 ℃ lower than the dew point temperature of the gas at the outlet of the compressor.
Compared with the prior art, the refining method of the gaseous methanol has the following advantages:
(1) The method for refining the gaseous methanol uses a double-tower rectification system consisting of a methanol tower, a recovery tower and a compressor to purify and separate the crude methanol gas containing impurities, and the high-temperature gas obtained by compression of the compressor can supply heat to a reboiler of the methanol tower and a reboiler of the recovery tower, so that the heat consumption is low, the condition that the heat is not required to be provided outside can be realized, the heat input of the methanol refining system is greatly reduced while the high-pressure gaseous refined methanol is ensured to be obtained, the compression ratio of the compressor is reduced, and the energy consumption of methanol refining is reduced.
(2) The method for refining gaseous methanol has the advantages of low compression ratio of the compressor, low manufacturing cost and low power consumption by using a single-stage compressor.
(3) According to the method for refining gaseous methanol, provided by the invention, through reasonable use of the compressor and reasonable division points, and through matching of operating conditions such as the operating pressure of the rectifying tower and the operating pressure of the recovery tower, the dual functions of heat pump heat supply and methanol gas pressurization are realized, and the method has the advantages of low compression ratio of the compressor, reduced heat consumption in methanol refining and the like.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention. In the drawings:
fig. 1 is a process flow diagram of a method for refining gaseous methanol (heating in series) according to an embodiment of the present invention.
Fig. 2 is a process flow diagram of a method for refining gaseous methanol (parallel heating) according to an embodiment of the present invention.
Reference numerals illustrate:
a 1-methanol column; a 2-compressor; 3-methanol tower reboiler; 4-a recovery tower; 5-a recovery column reboiler; 6-a recovery column condenser; 7-a recovery tower vacuum pump; 8-a heat exchanger; 9-methanol tower top pump; a 10-methanol tower kettle pump; 11-a recovery column overhead pump; 12-a recovery tower bottom pump;
a-crude methanol; b-refined methanol; c-waste liquid; d-exhaust gas.
Detailed Description
The invention will be described in detail below with reference to the drawings in connection with embodiments.
Example 1:
the flow rate of the crude methanol gas to be refined is 32600kg/h, the impurity is water, the water content is 1.84% (mass fraction, the same applies below), the rest is methanol, the methanol is purified into refined methanol gas with the concentration of not less than 99.97%, the pressure is not less than 2barg (gauge pressure, the same applies below), and meanwhile, the wastewater is discharged, and the methanol content in the wastewater is not more than 5%.
As shown in fig. 1, a method for refining gaseous methanol is described in the following specific flow:
(1) After the crude methanol a is fed into a heat exchanger 8 for heat exchange, the crude methanol a enters a methanol tower 1 for rectification separation, light component methanol is enriched at the tower top, heavy component water is enriched at the tower bottom, qualified refined methanol gas is obtained at the tower top, and a methanol-water mixture is obtained at the tower bottom;
(2) After the refined methanol vapor discharged from the top of the methanol tower 1 is compressed and the grade is improved by a compressor 2, the operating pressure, the operating temperature and the saturation temperature are all increased, the obtained high-grade gaseous methanol is divided into two paths, one path of gaseous methanol is discharged from a methanol refining device as a refined methanol product b after heat exchange and temperature adjustment by a heat exchanger 8, and the other path of gaseous methanol is supplied with heat by a reboiler 3 of the methanol tower;
(3) The mixed solution of methanol and water is extracted from the tower kettle of the methanol tower 1, pressurized by a tower kettle pump 10 of the methanol tower, and then sent to a recovery tower for further rectification, and the methanol in the mixed solution is recovered; in the recovery tower, water is further enriched in the tower bottom, and methanol is enriched in the tower top;
(4) The uncondensed compressed gas discharged from the methanol tower reboiler 3 is sent to the recovery tower reboiler 5 for further condensation, and condensate obtained by condensation is pressurized by the methanol tower top pump 9 and then is sent back to the top of the methanol tower 1 for reflux;
(5) Condensing the methanol-rich gas discharged from the top of the recovery tower 4 in a recovery tower condenser 6, pressurizing the obtained condensate (methanol-rich liquid) by a recovery tower top pump 11, and then dividing the condensate into two parts, wherein one part is returned to the top of the recovery tower 4 as a top reflux; one part is taken as the top of the tower and returns to the tower of the methanol tower 1, the recovery tower condenser 6 is vacuumized by the recovery tower vacuum pump 7, the recovery tower 4 is maintained to be in vacuum operation, and the vacuum pump 7 discharges waste gas d obtained by vacuumization out of the system;
(6) Waste liquid c (qualified waste water) is extracted from the tower bottom of the recovery tower 4, and is discharged out of the methanol refining system after being pressurized by a tower bottom pump 12 of the recovery tower.
After the system was running stably, the composition, temperature and pressure parameters of each stream are shown in tables 1 to 3.
Table 1 relevant operating parameters of each rectification column
Table 2 relevant operating parameters for each heat exchanger
Table 3 relevant operating parameters of the compressor
| An inlet | An outlet | Compression ratio | Power of | |
| Compressor 2 | 73.3℃，0.4barg | 138.3℃，2barg | 2.132 | 1635kW |
The purity of the refined methanol discharged from the methanol refining section is 99.97%, the pressure is 2barg, the temperature is 125.3 ℃, and the refined methanol can be returned to the upstream for recycling; the water content of the wastewater is 95 percent, and the wastewater can be discharged to a downstream wastewater treatment device. After the tower top gas of the methanol tower 1 is pressurized from 0.4barg to 2barg, the temperature reaches 138.3 ℃, the saturation temperature is 95.1 ℃, the mass fraction of water in the tower kettle of the methanol tower 1 is set to be 17.95%, and the heat transfer temperature difference of the reboiler 3 of the methanol tower is 17.1 ℃ at the moment, so that the heat transfer requirement is met; under the precondition that the methanol content in the tower bottom of the recovery tower 4 is lower than 5%, the tower top pressure of the recovery tower 4 is set to be-0.5 barg, and the heat exchange temperature difference of the recovery tower reboiler 5 is 17.4 ℃ at the moment, so that the heat transfer requirements are met.
The heat load of the reboiler 3 of the methanol tower and the heat load of the reboiler 5 of the recovery tower are 8441kW in total, the heat of the reboiler 3 of the methanol tower and the heat of the reboiler 5 of the recovery tower are provided by the outlet gas of the compressor 2, the externally provided steam is not required to be consumed, the power of the shaft of the compressor is 1635kW, which is equivalent to the power of the shaft of 1635kW, the heat consumption of the reboiler of 8441kW is replaced, the equivalent amount of the cold energy consumption required by condensing the top gas of the methanol tower 1 is also used for condensing, and meanwhile, the pressure of the methanol gas is increased, so that the methanol gas can be smoothly sent back to the upstream. The condensing temperature of the medium at the hot side of the recovery tower condenser 6 is 49 ℃, and circulating water in public engineering of the whole plant can be adopted for condensation.
The compression ratio (absolute ratio) of the compressor 2 is 2.132, namely the pressure of the gas at the top of the methanol tower is only required to be increased 2.132 times, so that heat can be supplied to the reboiler of the methanol tower and the reboiler of the recovery tower, the compressor can be a single-stage centrifugal compressor, a multi-stage compressor is not required, and the equipment cost and the operation cost can be reduced.
Example 2:
the flow rate of the crude methanol gas to be refined is 32600kg/h, the impurity is water, the water content is 1.84% (mass fraction, the same applies below), the rest is methanol, the methanol is purified into refined methanol gas with the concentration of not less than 99.97%, the pressure is not less than 2barg (gauge pressure, the same applies below), and meanwhile, the wastewater is discharged, and the methanol content in the wastewater is not more than 5%.
As shown in fig. 2, a method for refining gaseous methanol is described in the following specific flow:
(1) After the raw methanol a is fed into a heat exchanger 8 for heat exchange and temperature rise, the raw methanol a enters a methanol tower 1 for rectification separation, light component methanol is enriched at the tower top, heavy component water is enriched at the tower bottom, qualified refined methanol gas is obtained at the tower top, and a methanol-water mixture is obtained at the tower bottom;
(2) After the refined methanol vapor discharged from the top of the methanol tower 1 is compressed and upgraded by a compressor 2, the operating pressure, the operating temperature and the saturation temperature are all raised, the obtained high-grade gaseous methanol is divided into two paths, one path of gaseous methanol is discharged from a methanol refining device as a refined methanol product b after being subjected to temperature adjustment by a heat exchanger 8, and the other path of gaseous methanol is respectively supplied with heat for a methanol tower reboiler 3 and a recovery tower reboiler 5;
(3) The mixed solution of methanol and water is extracted from the tower kettle of the methanol tower 1, pressurized by a tower kettle pump 10 of the methanol tower, and then sent to a recovery tower for further rectification, and the methanol in the mixed solution is recovered; in the recovery tower, water is further enriched in the tower bottom, and methanol is enriched in the tower top;
(4) The methanol condensate discharged from the reboiler of the methanol tower and the reboiler of the recovery tower is pressurized by a pump 9 at the top of the methanol tower and then is completely returned to the top of the methanol tower 1 for reflux;
(5) Condensing the methanol-rich gas discharged from the top of the recovery tower 4 in a recovery tower condenser 6, pressurizing the obtained condensate (methanol-rich liquid) by a recovery tower top pump 11, and then dividing the condensate into two parts, wherein one part is returned to the top of the recovery tower 4 as a top reflux; one part is taken as the top of the tower and returns to the tower of the methanol tower 1, the recovery tower condenser 6 is vacuumized by the recovery tower vacuum pump 7, the recovery tower 4 is maintained to be in vacuum operation, and the vacuum pump 7 discharges waste gas d obtained by vacuumization out of the system;
(6) Waste liquid c (qualified waste water) is extracted from the tower bottom of the recovery tower 4, and is discharged out of the methanol refining system after being pressurized by a tower bottom pump 12 of the recovery tower.
The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, alternatives, and improvements that fall within the spirit and scope of the invention.
Claims (6)
1. A refining method of gaseous methanol is characterized in that: purifying and separating crude methanol gas containing impurities by using a double-tower rectification system consisting of a methanol tower, a recovery tower and a compressor, wherein in the refining process, high-temperature gas compressed by the compressor supplies heat to the methanol tower and also supplies heat to the recovery tower;
the refining method of the gaseous methanol comprises the following steps:
1) The crude methanol gas is sent to a methanol tower for separation, mixed liquid of methanol and impurities is extracted from the tower bottom of the methanol tower, and refined methanol gas is extracted from the tower top of the methanol tower;
2) The refined methanol gas extracted from the top of the methanol tower is pressurized by a compressor, the steam grade is improved to obtain high-grade gas, the high-grade gas supplies heat to a reboiler of the methanol tower and a reboiler of a recovery tower, and meanwhile, the pressurized gaseous methanol is extracted from an outlet of the compressor and is taken as refined methanol product to be sent out of a methanol refining system;
3) The mixed solution of methanol and impurities extracted from the tower bottom of the methanol tower is sent to a recovery tower for further separation, gas extracted from the tower top of the recovery tower is condensed to obtain methanol-rich solution, the methanol-rich solution is pressurized by a pump and is divided into two paths, one path is used as a return flow to the tower top of the recovery tower, the other path is used as a product at the tower top of the recovery tower to be sent back to the methanol tower, qualified waste liquid containing impurities is extracted from the tower bottom of the recovery tower, and the qualified waste liquid is sent out of a methanol refining system;
the heat required by the methanol tower reboiler and the recovery tower reboiler is provided by high-grade gas at the outlet of the compressor;
the operation pressure of the recovery tower is lower than that of the methanol tower, and under the operation pressure, the temperature of the bottom liquid of the recovery tower is lower than the saturation temperature of the gas at the outlet of the compressor;
the bubble point temperature of the bottom liquid of the recovery tower is 5-30 ℃ lower than the dew point temperature of the outlet gas of the compressor.
2. A method for refining gaseous methanol according to claim 1, wherein: the recovery tower is provided with a tower top condenser, and the gas at the tower top of the recovery tower is condensed and then is pressurized in a liquid phase form by a pump and then is returned to the methanol tower.
3. A method for refining gaseous methanol according to claim 1, wherein: the temperature of the methanol tower kettle liquid is lower than the saturation temperature of the gas at the outlet of the compressor.
4. A method for refining gaseous methanol according to claim 1, wherein: the crude methanol is fed in a gas phase, the refined methanol is discharged in a gas phase, and the refined methanol discharge pressure is higher than the crude methanol feed pressure.
5. A method for refining gaseous methanol according to claim 1, wherein: the methanol tower reboiler and the recovery tower reboiler can form a series heat supply passage or a parallel heat supply passage, and all condensate discharged by the methanol tower reboiler and the recovery tower reboiler is used as a return flow to be returned to the top of the methanol tower.
6. A method for refining gaseous methanol according to claim 1, wherein: the boiling point of the impurity is higher than that of methanol under the same pressure, and the impurity does not form a low azeotrope with methanol.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911398747.6A CN110963890B (en) | 2019-12-30 | 2019-12-30 | Refining method of gaseous methanol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911398747.6A CN110963890B (en) | 2019-12-30 | 2019-12-30 | Refining method of gaseous methanol |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110963890A CN110963890A (en) | 2020-04-07 |
| CN110963890B true CN110963890B (en) | 2024-04-16 |
Family
ID=70037424
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911398747.6A Active CN110963890B (en) | 2019-12-30 | 2019-12-30 | Refining method of gaseous methanol |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110963890B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111635293A (en) * | 2020-05-14 | 2020-09-08 | 天津市汇筑恒升科技有限公司 | Sodium methoxide production device and method |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101786940A (en) * | 2010-03-05 | 2010-07-28 | 惠生工程（中国）有限公司 | Methanol heat-pump rectifying process |
| 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 |
| CN207950711U (en) * | 2018-01-15 | 2018-10-12 | 苏州欧拉透平机械有限公司 | Energy-saving methanol rectifying system |
-
2019
- 2019-12-30 CN CN201911398747.6A patent/CN110963890B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101786940A (en) * | 2010-03-05 | 2010-07-28 | 惠生工程（中国）有限公司 | Methanol heat-pump rectifying process |
| 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 |
| CN207950711U (en) * | 2018-01-15 | 2018-10-12 | 苏州欧拉透平机械有限公司 | Energy-saving methanol rectifying system |
Non-Patent Citations (1)
| Title |
|---|
| 甲醇热泵精馏新工艺;叶鑫;吕建宁;丁干红;宫万福;;化工进展(S2);74-77 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN110963890A (en) | 2020-04-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101703840B (en) | Four-effect rectification system for synthesizing leather dimethyl formamide solution by wet method and recovery method | |
| CN104788289B (en) | A kind of pump coupled heat technique of ethylene glycol rectifying | |
| CN111437619B (en) | Multi-tower differential pressure energy-saving absolute alcohol distillation system and absolute alcohol energy-saving production method | |
| CN110028385B (en) | Method and device for separating isopropyl alcohol diisopropyl ether aqueous solution | |
| CN108409532B (en) | System and process for recycling solvent for producing glyphosate by alkyl ester method based on secondary condensation | |
| CN110963890B (en) | Refining method of gaseous methanol | |
| CN108083984B (en) | Method for recovering glyphosate solvent and byproducts | |
| CN102471194A (en) | Method and device for producing methanol and dimethyl ether | |
| CN111517920B (en) | Process for separating tetrahydrofuran-methanol-water by three-tower batch rectification | |
| CN111377801B (en) | Method and system for refining low carbon alcohol | |
| CN212152133U (en) | Refining plant of gaseous state methyl alcohol | |
| CN114797145B (en) | Differential pressure thermal coupling rectification process for coal-to-ethylene glycol byproduct | |
| CN216629706U (en) | Separation refining system device suitable for low-concentration organic solution | |
| CN216378008U (en) | System for producing low-residual alcohol monoalkyl fatty tertiary amine | |
| CN210030499U (en) | Cyclohexane separating device for producing cyclohexanone and cyclohexanol | |
| CN107778166A (en) | A kind of method of heat pump rectification system recovery of acetic acid from low-concentration acetic acid wastewater | |
| CN115124412B (en) | Energy-saving separation process for synthesizing butanone alcohol reaction liquid | |
| CN111635348A (en) | Application and system of screw vacuum pump in caprolactam refining process production | |
| CN107434757B (en) | Method and device for recycling caprolactam organic extractant with ultralow energy consumption | |
| CN111170826A (en) | Clean recovery system and clean recovery process for chloromethane in glyphosate production tail gas | |
| CN216725841U (en) | Heavy rectification device that takes off in ultrapure ammonia preparation system | |
| CN216236780U (en) | Production system for increasing yield of methylamine | |
| CN115253350B (en) | Double-tower MVR continuous distillation recovery system and method | |
| CN219722856U (en) | System for reducing steam consumption of methylamine device | |
| CN210974481U (en) | Device for improving concentration of phosgenation reaction phosgene |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| OL01 | Intention to license declared |