CN103387483A - Production device and process of methanol alkali metal salts - Google Patents
Production device and process of methanol alkali metal salts Download PDFInfo
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- CN103387483A CN103387483A CN2013103529135A CN201310352913A CN103387483A CN 103387483 A CN103387483 A CN 103387483A CN 2013103529135 A CN2013103529135 A CN 2013103529135A CN 201310352913 A CN201310352913 A CN 201310352913A CN 103387483 A CN103387483 A CN 103387483A
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- OKKJLVBELUTLKV-UHFFFAOYSA-N methanol Natural products OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 375
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 24
- 238000000034 method Methods 0.000 title claims abstract description 17
- -1 methanol alkali metal salts Chemical class 0.000 title claims abstract description 9
- 229910052783 alkali metal Inorganic materials 0.000 title abstract description 9
- 238000006243 chemical reaction Methods 0.000 claims abstract description 63
- 239000007788 liquid Substances 0.000 claims abstract description 43
- 239000003513 alkali Substances 0.000 claims abstract description 33
- 230000006835 compression Effects 0.000 claims description 19
- 238000007906 compression Methods 0.000 claims description 19
- 238000010438 heat treatment Methods 0.000 claims description 15
- 239000011552 falling film Substances 0.000 claims description 14
- 239000007791 liquid phase Substances 0.000 claims description 12
- 238000007600 charging Methods 0.000 claims description 8
- 239000006200 vaporizer Substances 0.000 claims description 8
- 238000007599 discharging Methods 0.000 claims description 5
- 230000000630 rising effect Effects 0.000 claims description 4
- 239000007921 spray Substances 0.000 claims description 4
- 238000002360 preparation method Methods 0.000 abstract description 9
- 239000000463 material Substances 0.000 abstract description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 47
- 235000011121 sodium hydroxide Nutrition 0.000 description 21
- 238000005516 engineering process Methods 0.000 description 11
- 239000007789 gas Substances 0.000 description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 8
- 239000007787 solid Substances 0.000 description 7
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 6
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 4
- 150000001340 alkali metals Chemical class 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 150000008044 alkali metal hydroxides Chemical class 0.000 description 3
- 238000004821 distillation Methods 0.000 description 3
- 238000005070 sampling Methods 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 238000003672 processing method Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
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Abstract
The invention relates to a production device and a preparation process of methanol alkali metal salts. The production device comprises a rectifying tower (1) and a reaction tower (3), wherein after methanol steam generated from the top of the rectifying tower (1) is compressed through at lease one steam compressor, one part of the methanol steam is introduced into a reboiler (2) to heat low-temperature materials circulated out of the bottom of the rectifying tower (1), while the other part of the methanol steam is separated by a gas-liquid separator (11) and then introduced into the reaction tower (3) to react with an alkali liquor; the steam on the top of the reaction tower (3) is introduced into the rectifying tower (1) and thereby recycled. According to the invention, the rectifying system and the reaction system are combined organically; the compressed methanol steam is utilized rationally, so that steam consumption at the rectifying stage and the reaction stage in the traditional process is greatly reduced; compared with the traditional process, the steam consumption of the production device and the preparation process per hour is more than 20% lower than that of the previous process.
Description
Technical field
The present invention relates to production equipment and the technique of an alkali metal salt in the Chemicals preparation field, especially relate to production equipment and the preparation technology of rosaline metal-salt.
Background technology
The rosaline metal-salt is the common agents of field of medicine and chemical technology, is used as the catalyzer of condensing agent, chemical reagent, food oils processing etc. in organic synthesis.What traditional rosaline metal-salt preparation technology adopted is that solid alkali metal oxyhydroxide and methanol solution are hybridly prepared into certain density alkali lye, the alkali lye that will prepare again reacts with methanol gas in reaction tower, keep stable reaction in reactive system, the rosaline metal-salt product introduction receiving tank of generation.
, by researching and analysing, find that traditional rosaline metal-salt preparation technology has the following disadvantages:
1, stage of rectification
Traditional technology needs to adopt steam to improve the rectifying tower temperature by reboiler heating alcohol liquid-like phase in the methanol rectification process, also need simultaneously a large amount of steam to pass into the rectifying tower chuck interior to keep temperature in tower, meanwhile the methanol vapor of rectifying tower tower top also needs a large amount of process waters to cool.
2, step of reaction
Traditional technology need to heat to improve temperature of reaction by reboiler to alkali lye with steam at methyl alcohol and alkaline reaction stage, also needs a certain amount of steam to keep the reaction tower interior reaction temperature simultaneously.
Summary of the invention
Order of the present invention is to provide a kind of production equipment and technique of rosaline metal-salt of high-efficiency low energy consumption, thereby overcomes the defect of the high energy consumption that exists in rosaline metal-salt production process in prior art.Purpose of the present invention can be achieved through the following technical solutions:
The invention provides a kind of production equipment of rosaline metal-salt, comprise rectifying tower and reaction tower, it is characterized in that:
The pipeline of described rectifying tower tower top methanol steam outlet is divided into two branches, and one of them branch is controlled and by vapour compressor A, with the reboiler steam entrance, is connected by switch-valve A;
Described tower bottom of rectifying tower bottom pipe is connected with the reboiler liquid inlet by reboiler circulation pump, and corresponding liquid exit is connected with tower bottom of rectifying tower;
Another branch in described rectifying tower push pipe road is controlled and by vapour compressor B, with gas-liquid separator, is connected by switch-valve B; The pneumatic outlet of gas-liquid separator is connected with the reaction tower tower reactor.
The present invention also provides the production equipment of another kind of rosaline metal-salt, comprises rectifying tower and reaction tower, it is characterized in that:
The pipeline of described rectifying tower tower top methanol steam outlet is controlled and is connected with vapour compressor A by switch-valve A;
Described tower bottom of rectifying tower bottom pipe is connected with the reboiler liquid inlet by reboiler circulation pump, and the corresponding outlet in reboiler bottom is connected with tower bottom of rectifying tower;
The outlet conduit of vapour compressor A is divided into two branches, and one of them branch is connected with the reboiler steam entrance; Another branch is connected with gas-liquid separator; The pneumatic outlet of gas-liquid separator is connected with the reaction tower tower reactor.
Above-mentioned any device of the present invention also comprises that following technical characterictic or its make up mutually:
Tower bottom of rectifying tower is connected with vaporizer;
Reboiler can be the various reboilers that can carry out the gas-liquid heat exchange, includes but not limited to: a kind of in board-like reboiler, falling-film reboiler or shell and tube reboiler; Preferred falling-film reboiler;
The outlet of reaction tower overhead gas is connected with tower bottom of rectifying tower by pipeline;
The liquid exit of reboiler bottom is connected with receiving tank;
The gas-liquid separator liquid exit is connected with receiving tank;
Receiving tank is connected with the rectifying tower tower top by recycle pump.
Corresponding with said apparatus, the present invention also provides a kind of production method of rosaline metal-salt, comprises the steps:
1), with the dissolve with methanol alkali metal hydroxide, prepare alkali lye;
2), industrial methanol is vaporized at tower bottom of rectifying tower; A part of methanol vapor of tower top passes into reboiler after compressor A compression, reboiler circulation pump pumps into reboiler with the Liquid Phase Methanol of tower bottom of rectifying tower bottom outflow simultaneously, after Liquid Phase Methanol and methanol vapor generation heat exchange, from reboiler, flow out and enter tower bottom of rectifying tower;
3), enter gas-liquid separator after the compressed machine B compression of another part methanol vapor of tower top, gaseous methanol passes into the reaction tower tower reactor;
4), reacting by heating tower tower reactor, alkali lye is from the charging of reaction tower top, with the methanol vapor reaction of from tower reactor, rising, the rosaline metal-salt that obtains is from discharging at the bottom of the reaction tower tower.
Corresponding with said apparatus, the present invention also provides the production method of another kind of rosaline metal-salt, comprises the steps:
1), with the dissolve with methanol alkali metal hydroxide, prepare alkali lye;
2), industrial methanol is vaporized at tower bottom of rectifying tower; The methanol vapor of tower top passes into reboiler through compressor A compression rear portion methanol vapor, reboiler circulation pump pumps into reboiler with the Liquid Phase Methanol of tower bottom of rectifying tower bottom outflow simultaneously, after Liquid Phase Methanol and methanol vapor generation heat exchange, from reboiler, flow out and enter tower bottom of rectifying tower;
3), another part methanol vapor after compressor A compression enters gas-liquid separator, gaseous methanol passes into the reaction tower tower reactor;
4), reacting by heating tower tower reactor, alkali lye is from the charging of reaction tower top, with the methanol vapor reaction of from tower reactor, rising, the rosaline metal-salt that obtains is from discharging at the bottom of the reaction tower tower.
Above-mentioned any means of the present invention also comprises that following technical characterictic or its make up mutually:
Reboiler can be the various reboilers that can carry out the gas-liquid heat exchange, includes but not limited to: a kind of in board-like reboiler, falling-film reboiler or shell and tube reboiler; Preferred falling-film reboiler;
The gas of reaction tower tower top output passes into tower bottom of rectifying tower through pipeline and recycles;
Methanol gas after compressed machine A compression carries out producing after heat exchange in reboiler refined methanol is collected with receiving tank;
Liquid refined methanol by gas-liquid separator separates is collected with receiving tank;
It is very useful in spray that a part of refined methanol in receiving tank is circulated to rectifying tower by recycle pump.
Beneficial effect
The present invention compresses the methanol vapor of rectifying tower tower top by at least one vapour compressor, the material that a part passes in reboiler the low temperature that recycles at the bottom of rectifying tower heats, after the heat exchange stable circulation, substantially the vaporizer preheating the unloading phase of can substituting distillation system, the steam consumption of minimizing stage of rectification; Another part passes in reaction tower and alkaline reaction after gas-liquid separator separates,, for reaction provides the part heat, guarantee that simultaneously certain pressure official post reaction tower overhead vapours can pass into tower bottom of rectifying tower and recycle.The present invention organically combines distillation system and reactive system, reasonable utilization by the methanol steam to after compression, greatly reduce the steam consumption of stage of rectification and step of reaction in traditional technology, with respect to traditional technology, the present invention per hour steam consumption has reduced more than 20% than original technique.
Description of drawings
Fig. 1 and Fig. 2 are device and the Production Flow Chart schematic diagram of the embodiment of the present invention 1 and embodiment 2 correspondences
In Fig. 1 and Fig. 2: 1 is methanol rectifying tower, and 2 is reboiler, and 3 is reaction tower, and 4 is reboiler circulation pump, and 5 is vaporizer, 6 is compressor A, and 7 is compressor B, and 8 is receiving tank, and 9 is gas-liquid separator, 10 is opening for feed, and 11 is recycle pump, and 12 is switch-valve A, and 13 is switch-valve B.
Embodiment
Below in conjunction with specific embodiment and Figure of description, traditional technology and the present invention are carried out detailed comparative illustration.
Solid alkali metal oxyhydroxide (sodium hydroxide or potassium hydroxide) is joined in alkali solving can, squeeze in alkali solving can with the methyl alcohol that fresh feed pump will necessarily measure, circulate and dissolve solid caustic soda, control temperature in alkali solving can with recirculated water, make it temperature and remain on 50 ℃, in alkali alcohol liquid, alkali metal hydroxide content reaches 20%, forms the qualified alkali lye of preparation standby.
Industrial methanol (methyl alcohol 99.5%, water 0.5%, 40 ℃ of temperature, flow 165kg/h) is passed into methanol evaporator 5, when liquid level reaches 90%, pass into 0.6Mpa, 160 ℃ of saturation steam heating of temperature in chuck, after heating, methyl alcohol is squeezed into rectifying tower 1, made methyl alcohol in rectifying tower 1 tower reactor gasification.After tower top pressure reached pressure-fired, methyl alcohol no longer entered rectifying tower 1 from vaporizer 5, changed from opening for feed 10 and entered rectifying tower 1; In operational process, monitor at any time tower top pressure, when tower top pressure was normal, industrial methanol was from opening for feed 10 chargings, and when tower top pressure was not enough, industrial methanol was from methanol evaporator 5 chargings.
Regulating rectifying tower 1 tower top temperature is 63 ℃, and pressure is 0.02Mpa, and (compressor A inlet temperature is 63 ℃ to compressor A 6 compression methanol vapor, and intake pressure is 0.03Mpa, and temperature out is 78 ℃, and top hole pressure is 0.64Mpa, and flow is 6400m
3/ h), methanol vapor after compression passes into falling-film reboiler 2, the low temperature liquid phase methyl alcohol that flows out from rectifying tower 1 tower reactor bottom pumps into from falling-film reboiler 2 tops through reboiler circulation pump 4, with the methanol vapor heat exchange after compression, the hot methanol circulation of from falling-film reboiler 2 bottoms, flowing out enters rectifying tower 1 tower reactor, thereby by methanol vapor and the heating that realizes rectifying tower 1 tower reactor methyl alcohol of the recycle methanol heat exchange in falling-film reboiler 2 of compression, the tower reactor temperature is 68 ℃.Along with compressor A 6 load increases gradually, regulate tower top temperature, pressure is qualified to refined methanol, qualified refined methanol enters receiving tank 8 after the heat exchange of reboiler gas-liquid.
Entering gas-liquid separator 9(compressor B inlet temperature after 7 pairs of a part of methanol vapor of compressor B are compressed is 62 ℃, and intake pressure is 0.03Mpa, and temperature out is 66 ℃, and top hole pressure is 0.08Mpa, and flow is 2400m
3/ h), gas-phase methanol after separation enters reaction tower 3 systems, qualified liquid phase refined methanol enters receiving tank 8, regulate compressor B 7 loads, until after two system stabilities, make the tower reactor temperature reach 90 ℃ to passing into steam heating in reaction tower 3 tower reactor chucks, pass into methanol gas reaction (methanol feeding amount: 9m in the alkali lye for preparing and tower
3/ h; Alkali lye inlet amount: 1.36m
3/ h), keep stable reaction in reactive system, reaction methanol an alkali metal salt product, enter corresponding receiving tank after the sampling chemical examination is qualified, and the mixed gas that comprises methyl alcohol and water vapor passes into rectifying tower 1 tower reactor from reaction tower 3 tower tops (78 ℃ of temperature) outlet by pipeline and recycles.As required, the refined methanol in receiving tank 8 is circulated to rectifying tower 1 tower top by recycle pump 11 and sprays.
By statistics, adopt processing method of the present invention, per hour steam flow is 13.88t/h.
Solid alkali metal oxyhydroxide (sodium hydroxide or potassium hydroxide) is joined in alkali solving can, squeeze in alkali solving can with the methyl alcohol that fresh feed pump will necessarily measure, circulate and dissolve solid caustic soda, control temperature in alkali solving can with recirculated water, make it temperature and remain on 50 ℃, in alkali alcohol liquid, alkali metal hydroxide content reaches 20%, forms the qualified alkali lye of preparation standby.
Industrial methanol (methyl alcohol 99.5%, water 0.5%, 40 ℃ of temperature, flow 165kg/h) is passed into methanol evaporator 5, when liquid level reaches 90%, pass into 0.6Mpa, 160 ℃ of saturation steam heating of temperature in chuck, after heating, methyl alcohol is squeezed into rectifying tower 1, made methyl alcohol in rectifying tower 1 tower reactor gasification.After tower top pressure reached pressure-fired, methyl alcohol no longer entered rectifying tower 1 from vaporizer 5, changed from opening for feed 10 and entered rectifying tower 1; In operational process, monitor at any time tower top pressure, when tower top pressure was normal, industrial methanol was from opening for feed 10 chargings, and when tower top pressure was not enough, industrial methanol was from methanol evaporator 5 chargings.
regulating rectifying tower 1 tower top temperature is 60 ℃, pressure is 0.012Mpa, (compressor A inlet temperature is 61 ℃ to compressor A 6 compression methanol vapor, intake pressure is 0.023Mpa, temperature out is 79 ℃, top hole pressure is 0.67Mpa, flow is 6300m3/h), a part of methanol vapor after compression is controlled and is passed into falling-film reboiler 2 by switch-valve A 12, the low temperature liquid phase methyl alcohol that flows out from rectifying tower 1 tower reactor bottom pumps into from falling-film reboiler 2 tops through reboiler circulation pump 4, with the heat exchange of compression methanol vapor, the hot methanol circulation of from falling-film reboiler 2 bottoms, flowing out enters rectifying tower 1 tower reactor, thereby methanol vapor and the heating that realizes rectifying tower 1 tower reactor methyl alcohol of the recycle methanol heat exchange in falling-film reboiler 2 by compression, the tower reactor temperature is 67 ℃.Along with compressor A 6 load increases gradually, regulate tower top temperature, pressure is qualified to refined methanol, qualified refined methanol enters receiving tank 8 after the heat exchange of reboiler gas-liquid.
Another part methanol vapor after compressor A 6 compressions is controlled and is entered gas-liquid separator 9 by switch-valve B 13, gas-phase methanol after separation enters reaction tower 3 systems, qualified liquid phase refined methanol enters receiving tank 8, until after two system stabilities, make the tower reactor temperature reach 90 ℃ to passing into steam heating in reaction tower 3 tower reactor chucks, pass into methanol gas reaction (methanol feeding amount: 8.6m in the alkali lye for preparing and tower
3/ h; Alkali lye inlet amount: 1.46m
3/ h), keep stable reaction in reactive system, reaction methanol an alkali metal salt product, enter corresponding receiving tank after the sampling chemical examination is qualified, and the mixed gas that comprises methyl alcohol and water vapor passes into rectifying tower 1 tower reactor from reaction tower 3 tower tops (78 ℃ of temperature) outlet by pipeline and recycles.As required, the refined methanol in receiving tank 8 is circulated to rectifying tower 1 tower top by recycle pump 11 and sprays.
By statistics, adopt processing method of the present invention, per hour steam flow is 14.79t/h.
The comparative example
Adopt traditional technology
Main technologic parameters is as follows:
Rectifying tower tower top temperature is 64 ℃, and tower top pressure is 0.015Mpa, and the tower reactor temperature is 72 ℃.
The reaction tower tower top temperature is 79 ℃, and the tower reactor temperature is 89 ℃.
Cover tower parameter of materials is
Methanol feeding amount: 7.6m
3/ h
Alkali lye inlet amount: 1.44m
3/ h
This technique comprises the following steps:
Solid alkali metal oxyhydroxide is joined in alkali solving can, squeeze in alkali solving can with the methyl alcohol that fresh feed pump will necessarily measure, circulate and dissolve solid caustic soda, control temperature in alkali solving can with recirculated water, make it temperature and remain on 48 ℃, in alkali alcohol liquid, alkali metal hydroxide content reaches 19%, forms the qualified alkali lye of preparation.Industrial methanol (methyl alcohol 99.5%, water 0.5%, temperature 45 C, flow 172kg/h) passes into the methanol rectifying tower tower reactor, when in tower, liquid level reaches 92%, pass into 0.6Mpa, 160 ℃ of saturation steam heating of temperature in chuck, make methyl alcohol vaporizing, open steam heating, start simultaneously to supplement methyl alcohol, make the tower top discharging and keep balance.After rectifying tower is stable, qualified anhydrous methanol is entered in the reaction tower vaporizer, open steam, allow methyl alcohol vaporizing enter reaction tower, and from reaction top gaseous phase pipeline, enter rectifying tower, when two column distillations reach balance, start to add alkali lye from tower top, keep stable system in reaction tower, the corresponding receiving tank of rosaline metal-salt product introduction after sampling analysis is qualified.
By statistics, adopt original technique, per hour steam flow is 18.66t/h.
Can be found out by above three embodiment contrast, adopt technique of the present invention, per hour steam consumption has reduced more than 20% than original technique, and this proves absolutely the device combination mode of the present invention that adopts, can greatly reduce the consumption of steam, reach energy-saving and cost-reducing purpose.
Claims (10)
1. the production equipment of a rosaline metal-salt, comprise rectifying tower (1) and reaction tower (3), it is characterized in that:
The pipeline of described rectifying tower (1) tower top methanol steam outlet is divided into two branches, and one of them branch is by vapour compressor A(6) be connected with reboiler (2) steam-in;
Described rectifying tower (1) still bottom pipe is connected with reboiler (2) liquid inlet by reboiler circulation pump (4), and corresponding liquid exit is connected with rectifying tower (1) tower reactor;
Another branch of described rectifying tower (1) tower top pipeline is by vapour compressor B(7) be connected with gas-liquid separator (9); The pneumatic outlet of gas-liquid separator (9) is connected with reaction tower (3) tower reactor.
2. the production equipment of a rosaline metal-salt, comprise rectifying tower (1) and reaction tower (3), it is characterized in that:
The pipeline and vapour compressor A(6 of the outlet of described rectifying tower (1) tower top methanol steam) be connected;
Described rectifying tower (1) tower reactor bottom pipe is connected with reboiler (2) liquid inlet by reboiler circulation pump (4), and the corresponding liquid exit in reboiler (2) bottom is connected with rectifying tower (1) tower reactor;
Vapour compressor A(6) outlet conduit is divided into two branches, and one of them branch is connected with reboiler (2) steam-in; Another branch is connected with gas-liquid separator (9); The pneumatic outlet of gas-liquid separator (9) is connected with reaction tower (3) tower reactor.
3. production equipment as claimed in claim 1 or 2 is characterized in that: also comprise vaporizer (5), described vaporizer (5) and rectifying tower (1) tower reactor be connected.
4. production equipment as claimed in claim 3 is characterized in that: described reboiler (2) is selected from a kind of in board-like reboiler, falling-film reboiler or shell and tube reboiler.
5. production equipment as claimed in claim 1 or 2 is characterized in that: the overhead gas outlet of described reaction tower (3) is connected with rectifying tower (1) tower reactor by pipeline.
6. production equipment as claimed in claim 1 or 2, it is characterized in that: the liquid exit of reboiler (2) bottom is connected with receiving tank (8); Gas-liquid separator (9) liquid exit is connected with receiving tank (8); Receiving tank (8) is connected with rectifying tower (1) tower top by recycle pump (11).
7. the production method of a rosaline metal-salt, comprise the steps:
1), with the dissolve with methanol alkali metal hydroxide, prepare alkali lye;
2), industrial methanol is vaporized in rectifying tower (1) tower reactor; A part of methanol vapor of tower top is through compressor A(6) compression after pass into reboiler (2), reboiler circulation pump (4) pumps into reboiler (2) with the Liquid Phase Methanol of rectifying tower (1) tower reactor bottom outflow simultaneously, after Liquid Phase Methanol and methanol vapor generation heat exchange, from reboiler (2), flow out and enter tower bottom of rectifying tower;
3), the compressed machine B(7 of another part methanol vapor of tower top) enter gas-liquid separator (9) after compression, gaseous methanol passes into reaction tower (3) tower reactor;
4), reacting by heating tower (3) tower reactor, alkali lye is from reaction tower (3) top charging, with the methanol vapor reaction of from tower reactor, rising, the rosaline metal-salt that obtains is from discharging at the bottom of reaction tower (3) tower.
8. the production method of a rosaline metal-salt, comprise the steps:
1), with the dissolve with methanol alkali metal hydroxide, prepare alkali lye;
2), industrial methanol is vaporized in rectifying tower (1) tower reactor; The methanol vapor process compressor A(6 of tower top) compression rear portion methanol vapor passes into reboiler (2), reboiler circulation pump (4) pumps into reboiler (2) with the Liquid Phase Methanol of rectifying tower (1) tower reactor bottom outflow simultaneously, after Liquid Phase Methanol and methanol vapor generation heat exchange, from reboiler (2), flow out and enter rectifying tower (1) tower reactor;
3), compressor A(6) compression after another part methanol vapor enter gas-liquid separator (9), gaseous methanol passes into reaction tower (3) tower reactor;
4), reacting by heating tower (3) tower reactor, alkali lye is from the charging of reaction tower top, with the methanol vapor reaction of from tower reactor, rising, the rosaline metal-salt that obtains is from discharging at the bottom of reaction tower (3) tower.
9. production method as described in claim 6 or 7, it is characterized in that: described reboiler (2) is selected from: a kind of in board-like reboiler, falling-film reboiler or shell and tube reboiler.
10. production method as described in claim 6 or 7 is characterized in that: the gas of reaction tower (3) tower top output passes into rectifying tower (1) tower reactor through pipeline and recycles; The refined methanol that reboiler (2) and gas-liquid separator (9) flow out is collected by receiving tank (8); A part of refined methanol in receiving tank (8) is circulated to rectifying tower (1) tower top by recycle pump (11) and is used for spray.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110551003A (en) * | 2018-05-31 | 2019-12-10 | 杨祖杰 | System and process for preparing sodium methoxide by heat pump compression circulation double towers |
| 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 |
| CN112250545A (en) * | 2020-09-18 | 2021-01-22 | 安徽金邦医药化工有限公司 | Reaction system for sodium methoxide alkaline production and application method thereof |
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| CN102333575A (en) * | 2009-02-26 | 2012-01-25 | 巴斯夫欧洲公司 | Method for the distillative processing of a methanol/water mixture and method for producing alkali methylates |
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| CN1409696A (en) * | 1999-12-08 | 2003-04-09 | 巴斯福股份公司 | Method for producing alkali methylates |
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| CN110551003A (en) * | 2018-05-31 | 2019-12-10 | 杨祖杰 | System and process for preparing sodium methoxide by heat pump compression circulation double towers |
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| CN112250545A (en) * | 2020-09-18 | 2021-01-22 | 安徽金邦医药化工有限公司 | Reaction system for sodium methoxide alkaline production and application method thereof |
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|---|---|
| CN103387483B (en) | 2015-06-17 |
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