CN110963890A - Refining method of gaseous methanol - Google Patents
Refining method of gaseous methanol Download PDFInfo
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- CN110963890A CN110963890A CN201911398747.6A CN201911398747A CN110963890A CN 110963890 A CN110963890 A CN 110963890A CN 201911398747 A CN201911398747 A CN 201911398747A CN 110963890 A CN110963890 A CN 110963890A
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 633
- 238000007670 refining Methods 0.000 title claims abstract description 36
- 238000000034 method Methods 0.000 title claims abstract description 34
- 238000011084 recovery Methods 0.000 claims abstract description 87
- 239000012535 impurity Substances 0.000 claims abstract description 18
- 230000006835 compression Effects 0.000 claims abstract description 10
- 238000007906 compression Methods 0.000 claims abstract description 10
- 239000007788 liquid Substances 0.000 claims description 31
- 230000008569 process Effects 0.000 claims description 8
- 238000010992 reflux Methods 0.000 claims description 7
- 238000007599 discharging Methods 0.000 claims description 6
- 239000012071 phase Substances 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 239000002699 waste material Substances 0.000 claims description 5
- 238000009835 boiling Methods 0.000 claims description 3
- 239000007791 liquid phase Substances 0.000 claims description 2
- 230000008901 benefit Effects 0.000 abstract description 5
- 239000007789 gas Substances 0.000 description 54
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 13
- 239000002351 wastewater Substances 0.000 description 8
- WQDUMFSSJAZKTM-UHFFFAOYSA-N Sodium methoxide Chemical compound [Na+].[O-]C WQDUMFSSJAZKTM-UHFFFAOYSA-N 0.000 description 6
- 239000011259 mixed solution Substances 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- GBMDVOWEEQVZKZ-UHFFFAOYSA-N methanol;hydrate Chemical compound O.OC GBMDVOWEEQVZKZ-UHFFFAOYSA-N 0.000 description 4
- 239000000047 product Substances 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
- 238000010438 heat treatment 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
- 238000005265 energy consumption Methods 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
- 239000000463 material Substances 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
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- 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
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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
- Y02P20/50—Improvements relating to the production of bulk chemicals
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- 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 refined methanol gas, and heat is supplied to the methanol tower and the recovery tower after the grade of methanol steam is improved. The invention realizes the double functions of heat supply of the heat pump and methanol gas pressurization by reasonably using the compressor, setting a reasonable division point and reasonably matching the operating pressures of the two towers, and has the advantages of low compression ratio of the compressor, low heat consumption for 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 chemicals. When methanol is used as a stripping agent, gaseous methanol strips impurities from the liquid chemical, which are transferred from the liquid chemical to the gaseous methanol. The methanol is not consumed, so that a methanol refining system is required to be matched at the downstream of the stripping system, the crude methanol gas discharged from the stripping tower is separated, refined and recycled, impurities are removed, and the crude methanol gas is returned to the stripping system for recycling after the crude methanol gas reaches qualified purity. Since the process is a cyclic process, power must be introduced into the cycle to ensure stable operation of the cycle, i.e., pressurization of the methanol is required.
For example, methanol is adopted as a stripping agent in the production process of sodium methoxide, and the byproduct water of the synthesis reaction is continuously stripped from the reaction system by gas-phase methanol, so that the smooth proceeding of the reaction is ensured; the stripped crude methanol gas is refined and pressurized and then returned to the upstream for recycling. Because the stripping methanol in the production process of sodium methoxide is large in dosage and high in purity, a large amount of energy is consumed in the refining process of methanol, and the production cost of sodium methoxide is greatly increased. The methanol refining generally adopts a rectification method, if the ordinary rectification is adopted, qualified liquid methanol needs to be extracted, then a pump is used for boosting pressure, and finally high-pressure gas can be obtained through heating and vaporization, and a large amount of heat is consumed in the rectification and vaporization processes; if the common heat pump rectification is adopted, a compressor with a high compression ratio is required, and the construction cost and the operation cost are increased.
Disclosure of Invention
In view of the above, the present invention aims to provide a method for refining gaseous methanol, which can greatly reduce the heat input of a methanol refining system and reduce the compression ratio of a compressor while ensuring that high-pressure gaseous refined methanol is obtained, thereby reducing the energy consumption for refining methanol, reducing the production cost, saving energy, and having good economic and social benefits.
In order to achieve the purpose, the technical scheme of the invention is realized as follows:
a process for refining gaseous methanol features that a dual-tower rectifying system consisting of methanol tower, recovery tower and compressor is used to purify and separate the coarse methanol gas containing impurities, and the high-temp gas compressed by compressor can supply both heat to methanol tower and heat to recovery tower.
Further, the method comprises the following steps:
the double-tower rectifying system comprises a methanol tower reboiler and a recovery tower reboiler, the methanol tower reboiler is communicated with the methanol tower, a loop is formed between the methanol tower reboiler and the methanol tower, and the recovery tower reboiler is communicated with the recovery tower, and a loop is formed between the recovery tower reboiler and the recovery tower.
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 and the steam grade is promoted 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 simultaneously a strand of pressurized gaseous methanol is extracted from an outlet of the compressor and is taken as a refined methanol product to be sent out of a methanol refining system;
the mixed liquid of the methanol and the impurities extracted from the tower bottom of the methanol tower is sent to a recovery tower for further separation, the gas extracted from the tower top of the recovery tower is condensed to obtain methanol-rich liquid, and the qualified waste liquid containing the impurities is extracted from the tower bottom of the recovery tower and sent out of a methanol refining system.
Further, the heat required by the methanol tower reboiler and the recovery tower reboiler is provided by the high-grade gas at the outlet of the compressor.
Further, the operating pressure of the recovery tower is lower than that of the methanol tower, and the temperature of the recovery tower bottom liquid is lower than the saturation temperature of the outlet gas of the compressor at the operating pressure. 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 reboiler of the recovery tower.
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, the methanol-rich liquid is pressurized by a pump, one part of the methanol-rich liquid is delivered to the top of the recovery tower as a reflux, and the other part of the methanol-rich liquid is delivered to the methanol tower as a product at the top of the recovery tower.
The tower top gas of the recovery tower is condensed and then is sent back to the methanol tower in a liquid phase form through a pump under pressure, but not directly sent back to the methanol tower in a gas phase form, so that the operating pressure of the recovery tower can be lower than that of the methanol tower, and the temperature of a tower kettle of the recovery tower can be further reduced.
Further, the temperature of the methanol tower bottom liquid is lower than the saturation temperature of the gas at the outlet of the compressor.
The composition of the methanol tower kettle liquid meets the requirement that the temperature of the methanol tower kettle liquid is lower than the saturation temperature of the gas at the outlet of the compressor under the composition, and the requirement of heat transfer temperature difference is met at the moment, so that the high-pressure high-temperature gas at the outlet of the compressor can supply heat to the methanol tower reboiler.
Further, the crude methanol feeding is gas phase feeding, the fine methanol discharging is gas phase discharging, and the fine methanol discharging pressure is higher than the crude methanol feeding pressure.
Furthermore, the reboiler of the methanol tower and the reboiler of the recovery tower can form a series heat supply path or a parallel heat supply path, and all the condensate discharged by the reboiler of the methanol tower and the reboiler of the recovery tower is returned to the top of the methanol tower as reflux.
Further, the serial heat supply path refers to that the high-grade gas at the outlet of the compressor enters the reboiler of the methanol tower and the reboiler of the recovery tower in series to supply heat, and the parallel heat supply path refers to that the high-grade gas at the outlet of the compressor enters the reboiler of the methanol tower and the reboiler of the recovery tower in parallel to supply heat.
Further, the boiling point of the impurity is higher than that of methanol at the same pressure, and the impurity does not form a low azeotrope with methanol. Such as water and the like.
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 temperature difference design 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 recovery column bottoms is 15 ℃ or 20 ℃ lower than the dew point temperature of the compressor outlet gas.
Compared with the prior art, the refining method of the gaseous methanol has the following advantages:
(1) the invention relates to a refining method of gaseous methanol, which 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, high-temperature gas obtained by compression of the compressor can supply heat to a reboiler of the methanol tower and can supply heat to the reboiler of the recovery tower, the heat consumption is low, even external heat supply is not needed, the high-pressure gaseous refined methanol is ensured to be obtained, meanwhile, the heat input of the methanol refining system is greatly reduced, the compression ratio of the compressor is reduced, and therefore, the energy consumption for refining the methanol is reduced.
(2) The refining method of gaseous methanol has the advantages of low compression ratio of the compressor, low manufacturing cost and low power consumption, and can meet the requirements by using a single-stage compressor.
(3) According to the refining method of the gaseous methanol, disclosed by the invention, the compressor is reasonably used, the reasonable division point is set, and the operating conditions such as the operating pressure of the rectifying tower and the operating pressure of the recovery tower are matched, so that the double functions of heat supply of a heat pump and methanol gas pressurization are realized, and the advantages of low compression ratio of the compressor, reduced heat consumption of methanol refining and the like are achieved.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate an embodiment of the invention and, together with the description, serve to explain the invention and not to limit 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.
Description of reference numerals:
1-a methanol column; 2-a compressor; a 3-methanol column reboiler; 4-a recovery column; 5-recovery column reboiler; 6-recovery tower condenser; 7-recovery tower vacuum pump; 8-a heat exchanger; 9-methanol tower top pump; 10-methanol tower kettle pump; 11-a recovery tower overhead pump; 12-a recovery tower kettle pump;
a-crude methanol; b-refined methanol; c-waste liquor; d-exhaust gas.
Detailed Description
The present invention will be described in detail below with reference to the embodiments with reference to the attached drawings.
Example 1:
the flow rate of crude methanol gas to be refined is 32600kg/h, the impurity is water, the water content is 1.84% (mass fraction, the same below), the rest is methanol, the crude methanol gas 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 below), and simultaneously, waste water is discharged, and the methanol content in the waste water is not more than 5%.
As shown in fig. 1, a method for refining gaseous methanol is described as follows:
(1) after heat exchange is carried out on the crude methanol a fed material in a heat exchanger 8, 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 refined methanol steam discharged from the top of the methanol tower 1 is compressed by a compressor 2 and the grade is improved, the operation pressure, the operation temperature and the saturation temperature are all increased, the obtained high-grade gas methanol is divided into two paths, one path of methanol is sent to a heat exchanger 8 for heat exchange and temperature adjustment and then is discharged out of a methanol refining device as a refined methanol product b, and the other path of methanol is supplied with heat by a methanol removal tower reboiler 3;
(3) collecting methanol-water mixed solution from the bottom of a methanol tower 1, pressurizing the mixed solution by a methanol tower bottom pump 10, and sending the mixed solution to a recovery tower 2 for further rectification to recover methanol therein; in the recovery tower 2, water is further enriched in the tower kettle, and methanol is enriched in the tower top;
(4) the uncondensed compressed gas discharged from the methanol tower reboiler 3 is sent to a recovery tower reboiler 5 for further condensation, and the condensed liquid is pressurized by a methanol tower top pump 9 and then is completely 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, dividing the condensate into two parts, and returning one part of the condensate to the top of the recovery tower 4 as tower top reflux; one strand is taken as the top of the tower and is returned to the tower of the methanol tower 1, a condenser 6 of the recovery tower is vacuumized by a vacuum pump 7 of the recovery tower, the recovery tower 4 is maintained to be in vacuum operation, and the vacuum pump 7 discharges the waste gas d obtained by vacuumizing out of the system;
(6) waste liquid c (qualified waste water) is extracted from the tower bottom of the recovery tower 4, is pressurized by a tower bottom pump 12 of the recovery tower and then is discharged out of the methanol refining system.
When the system was operating stably, the composition of each stream and the temperature and pressure parameters are shown in tables 1-3.
TABLE 1 relevant operating parameters for the rectification columns
TABLE 2 relevant operating parameters for each Heat exchanger
TABLE 3 relevant operating parameters of the compressor
| Inlet port | An outlet | Compression ratio | Power of | |
| Compressor 2 | 73.3℃，0.4barg | 138.3℃，2barg | 2.132 | 1635kW |
The refined methanol separated in the methanol refining section has the purity of 99.97 percent, the pressure of 2barg and the temperature of 125.3 ℃, and 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 top gas of the methanol tower 1 is pressurized to 2barg from 0.4barg, 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 percent, and the heat transfer temperature difference of a 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 pressure at the top of the recovery tower 4 is set to-0.5 barg, and the heat exchange temperature difference of the reboiler 5 of the recovery tower is 17.4 ℃, so that the heat transfer requirements are met.
The heat load of the methanol tower reboiler 3 and the heat load of the recovery tower reboiler 5 are summed to be 8441kW, the heat of the two are provided by the outlet gas of the compressor 2, the steam provided by the outside is not required to be consumed, the shaft power of the compressor is 1635kW, which is equivalent to the shaft power of 1635kW, the heat consumption of the reboiler of 8441kW and the equivalent cold consumption required by condensing the tower top gas of the methanol tower 1 are replaced, and simultaneously, the pressure of the methanol gas is also improved, so that the methanol gas can be smoothly sent back to the upstream. The condensation temperature of the medium at the hot side of the condenser 6 of the recovery tower is 49 ℃, and the circulating water in the whole plant public works can be adopted for condensation.
The compression ratio (absolute pressure ratio) of the compressor 2 is only 2.132, namely the pressure of the gas at the top of the methanol tower only needs to be increased by 2.132 times, and heat can be supplied to the reboiler of the methanol tower and the reboiler of the recovery tower, so that the compressor can adopt a single-stage centrifugal compressor without selecting a multi-stage compressor, the equipment cost can be reduced, and the operation cost can also be reduced.
Example 2:
the flow rate of crude methanol gas to be refined is 32600kg/h, the impurity is water, the water content is 1.84% (mass fraction, the same below), the rest is methanol, the crude methanol gas 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 below), and simultaneously, waste water is discharged, and the methanol content in the waste water is not more than 5%.
As shown in fig. 2, a method for refining gaseous methanol is described as follows:
(1) feeding crude methanol a into a heat exchanger 8 for heat exchange and temperature rise, and then feeding the crude methanol a into a methanol tower 1 for rectification separation, wherein 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 steam discharged from the top of the methanol tower 1 is compressed by a compressor 2 and the grade is improved, the operation pressure, the operation temperature and the saturation temperature are all increased, the obtained high-grade gas methanol is divided into two paths, one path of the high-grade gas methanol is sent to a heat exchanger 8 for temperature adjustment and then is discharged out of a methanol refining device as a refined methanol product b, and the other path of the high-grade gas methanol is sent to a methanol tower reboiler 3 and a recovery tower reboiler 5 for heat supply respectively;
(3) collecting methanol-water mixed solution from the bottom of a methanol tower 1, pressurizing the mixed solution by a methanol tower bottom pump 10, and sending the mixed solution to a recovery tower 2 for further rectification to recover methanol therein; in the recovery tower 2, water is further enriched in the tower kettle, and methanol is enriched in the tower top;
(4) methanol condensate discharged from a reboiler of the methanol tower and a reboiler of the recovery tower is pressurized by a pump 9 at the top of the methanol tower and then is completely 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, dividing the condensate into two parts, and returning one part of the condensate to the top of the recovery tower 4 as tower top reflux; one strand is taken as the top of the tower and is returned to the tower of the methanol tower 1, a condenser 6 of the recovery tower is vacuumized by a vacuum pump 7 of the recovery tower, the recovery tower 4 is maintained to be in vacuum operation, and the vacuum pump 7 discharges the waste gas d obtained by vacuumizing out of the system;
(6) waste liquid c (qualified waste water) is extracted from the tower bottom of the recovery tower 4, is pressurized by a tower bottom pump 12 of the recovery tower and then is discharged out of the methanol refining system.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (10)
1. A method for refining gaseous methanol is characterized in that: a double-tower rectifying system consisting of a methanol tower, a recovery tower and a compressor is used for purifying and separating crude methanol gas containing impurities, and high-temperature gas obtained by compression of the compressor supplies heat to the methanol tower and the recovery tower in the refining process.
2. The method according to claim 1, wherein: the method 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 and the steam grade is promoted 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 simultaneously the pressurized gaseous methanol extracted from the outlet of the compressor is taken as a refined methanol product and sent out of a methanol refining system;
3) the mixed liquid of methanol and impurities extracted from the tower bottom of the methanol tower is sent to a recovery tower for further separation, the gas extracted from the tower top of the recovery tower is condensed to obtain methanol-rich liquid, the methanol-rich liquid is pressurized by a pump and then divided into two paths, one path of the methanol-rich liquid is sent to the tower top of the recovery tower as a return flow, the other path of the methanol-rich liquid is sent back to the methanol tower as a product at the tower top of the recovery tower, and qualified waste liquid containing the impurities is extracted from the tower bottom of the recovery tower and sent out of a methanol refining.
3. The method according to claim 2, wherein: the heat required by the reboiler of the methanol tower and the reboiler of the recovery tower is provided by high-grade gas at the outlet of the compressor.
4. The method according to claim 2, wherein: the operating pressure of the recovery tower is lower than that of the methanol tower, and the temperature of the recovery tower bottom liquid is lower than the saturation temperature of the outlet gas of the compressor under the operating pressure.
5. The method according to claim 2, wherein: the recovery tower is provided with a tower top condenser, and the tower top gas of the recovery tower is sent back to the methanol tower after being condensed and pressurized by a pump in a liquid phase form.
6. The method according to claim 2, wherein: the temperature of the methanol tower bottom liquid is lower than the saturation temperature of the gas at the outlet of the compressor.
7. The method according to claim 2, wherein: the coarse methanol feeding is gas phase feeding, the fine methanol discharging is gas phase discharging, and the fine methanol discharging pressure is higher than the coarse methanol feeding pressure.
8. The method according to claim 2, wherein: the reboiler of the methanol tower and the reboiler of the recovery tower can form a series heat supply path or a parallel heat supply path, and all the condensate discharged by the reboiler of the methanol tower and the reboiler of the recovery tower is used as reflux to be sent back to the top of the methanol tower.
9. The method according to claim 2, wherein: the boiling point of the impurities is higher than the boiling point of methanol at the same pressure, and the impurities do not form a low azeotrope with methanol.
10. The method according to claim 4, wherein: the bubble point temperature of the recovery tower bottom liquid is 5-30 ℃ lower than the dew point temperature of the gas at the outlet of the compressor.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| 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 |
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| CN101786940A (en) * | 2010-03-05 | 2010-07-28 | 惠生工程（中国）有限公司 | Methanol heat-pump rectifying process |
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