CN103387483B - 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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- CN103387483B CN103387483B CN201310352913.5A CN201310352913A CN103387483B CN 103387483 B CN103387483 B CN 103387483B CN 201310352913 A CN201310352913 A CN 201310352913A CN 103387483 B CN103387483 B CN 103387483B
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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 23
- -1 methanol alkali metal salts Chemical class 0.000 title claims abstract description 10
- 238000000034 method Methods 0.000 title abstract description 17
- 229910052783 alkali metal Inorganic materials 0.000 title abstract description 5
- 238000006243 chemical reaction Methods 0.000 claims abstract description 57
- 239000007788 liquid Substances 0.000 claims abstract description 43
- 239000003513 alkali Substances 0.000 claims abstract description 33
- 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
- 230000006835 compression Effects 0.000 claims description 10
- 238000007906 compression Methods 0.000 claims description 10
- 239000006200 vaporizer Substances 0.000 claims description 10
- 238000007599 discharging Methods 0.000 claims description 5
- 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
- 150000008044 alkali metal hydroxides Chemical class 0.000 description 7
- 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
- 239000012071 phase Substances 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 238000004821 distillation Methods 0.000 description 3
- 238000005070 sampling Methods 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 238000003672 processing method Methods 0.000 description 2
- 150000003839 salts Chemical class 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
- 230000000052 comparative effect Effects 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
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
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 Chemicals preparation field, especially relate to production equipment and the preparation technology of rosaline metal-salt.
Background technology
Rosaline metal-salt is the common agents of field of medicine and chemical technology, is used as the catalyzer etc. of condensing agent, chemical reagent, food oils process in organic synthesis.What traditional rosaline metal-salt preparation technology adopted is that solid alkali metal hydroxide and methanol solution are hybridly prepared into certain density alkali lye, again the alkali lye prepared is reacted with methanol gas in reaction tower, keep stable reaction in reactive system, the rosaline metal salt product of generation enters receiving tank.
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 rectifying tower temperature by reboiler heating alcohol liquid-like phase in methanol rectification process, also need a large amount of steam to pass into maintain temperature in tower in rectifying tower chuck, meanwhile the methanol vapor of rectifying tower tower top also needs a large amount of process waters to cool simultaneously.
2, step of reaction
Traditional technology needs to be heated to alkali lye by reboiler with steam to improve temperature of reaction at methyl alcohol and alkaline reaction stage, also needs a certain amount of steam to maintain reaction tower interior reaction temperature simultaneously.
Summary of the invention
Order of the present invention is production equipment and the technique of the rosaline metal-salt providing a kind of high-efficiency low energy consumption, thus overcomes the defect of the high energy consumption existed in rosaline metal-salt production process in prior art.Object 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 Liang Ge branch, and one of them branch is controlled by switch-valve A and is connected with reboiler steam entrance by vapour compressor A;
Described tower bottom of rectifying tower bottom pipe is connected with 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 by switch-valve B and is connected with gas-liquid separator by vapour compressor B; The pneumatic outlet of gas-liquid separator is connected with 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 to be connected with vapour compressor A by switch-valve A;
Described tower bottom of rectifying tower bottom pipe is connected with reboiler liquid inlet by reboiler circulation pump, and bottom reboiler, corresponding outlet is connected with tower bottom of rectifying tower;
The outlet conduit of vapour compressor A is divided into Liang Ge branch, and one of them branch is connected with reboiler steam entrance; Another branch is connected with gas-liquid separator; The pneumatic outlet of gas-liquid separator is connected with reaction tower tower reactor.
Above-mentioned any device of the present invention also comprises following technical characteristic or it combines mutually:
Tower bottom of rectifying tower is connected with vaporizer;
Reboiler can be the various reboilers that can carry out vapor liquid heat exchange, includes but not limited to: the one 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;
Gas-liquid separator liquid exit is connected with receiving tank;
Receiving tank is connected with 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), alkali lye is prepared with dissolve with methanol alkali metal hydroxide;
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 compresses, the Liquid Phase Methanol flowed out bottom tower bottom of rectifying tower is pumped into reboiler by reboiler circulation pump simultaneously, after Liquid Phase Methanol and methanol vapor generation heat exchange, flow out from reboiler and enter tower bottom of rectifying tower;
3), another part methanol vapor of tower top enters gas-liquid separator after compressor B compresses, and gaseous methanol passes into reaction tower tower reactor;
4), reacting by heating tower tower reactor, alkali lye, from the charging of reaction tower top, reacts with the methanol vapor risen from tower reactor, and the rosaline metal-salt obtained is from discharging at the bottom of 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), alkali lye is prepared with dissolve with methanol alkali metal hydroxide;
2), industrial methanol is vaporized at tower bottom of rectifying tower; The methanol vapor of tower top is compressed rear portion methanol vapor through compressor A and is passed into reboiler, the Liquid Phase Methanol flowed out bottom tower bottom of rectifying tower is pumped into reboiler by reboiler circulation pump simultaneously, after Liquid Phase Methanol and methanol vapor generation heat exchange, flow out from reboiler and enter tower bottom of rectifying tower;
3), compressor A compress after another part methanol vapor enter gas-liquid separator, gaseous methanol passes into reaction tower tower reactor;
4), reacting by heating tower tower reactor, alkali lye, from the charging of reaction tower top, reacts with the methanol vapor risen from tower reactor, and the rosaline metal-salt obtained is from discharging at the bottom of reaction tower tower.
Above-mentioned any means of the present invention also comprises following technical characteristic or it combines mutually:
Reboiler can be the various reboilers that can carry out vapor liquid heat exchange, includes but not limited to: the one 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 piping and recycles;
The refined methanol receiving tank produced after methanol gas after compressor A compresses carries out heat exchange in reboiler is collected;
Collected by the liquid refined methanol receiving tank of gas-liquid separator separates;
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 is compressed by the methanol vapor of at least one vapour compressor to rectifying tower tower top, a part passes in reboiler and heats the material of the low temperature recycled at the bottom of rectifying tower, after recuperated cycle is stable, substantially can substitute the vaporizer preheating unloading phase of distillation system, reduce the steam consumption of stage of rectification; Another part pass into after gas-liquid separator separates in reaction tower with alkaline reaction, for reaction partial heat is provided, ensure that certain pressure official post reaction tower overhead vapours can pass into tower bottom of rectifying tower and recycle simultaneously.Distillation system and reactive system organically combine by the present invention, by the Appropriate application to the methanol steam after compression, greatly reduce the steam consumption of stage of rectification and step of reaction in traditional technology, relative to traditional technology, the present invention's steam consumption per hour reduces more than 20% than original technique.
Accompanying drawing explanation
Fig. 1 and Fig. 2 is device and the Production Flow Chart schematic diagram of the embodiment of the present invention 1 and embodiment 2 correspondence
In Fig. 1 and Fig. 2: 1 is methanol rectifying tower, 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, detailed comparisons's explanation is carried out to traditional technology and the present invention.
Embodiment 1
Solid alkali metal hydroxide (sodium hydroxide or potassium hydroxide) is joined in alkali solving can, with fresh feed pump, the methyl alcohol necessarily measured is squeezed in alkali solving can, carry out circulation and dissolve solid caustic soda, temperature in alkali solving can is controlled with recirculated water, make it temperature and remain on 50 DEG C, in alkali alcohol liquid, alkali metal hydroxide content reaches 20%, and the alkali lye forming preparation qualified is for subsequent use.
Industrial methanol (methyl alcohol 99.5%, water 0.5%, temperature 40 DEG C, flow 165kg/h) is passed into methanol evaporator 5, when liquid level reaches 90% time, 0.6Mpa, temperature 160 DEG C of saturation steam heating are passed in chuck, after heating, methyl alcohol is squeezed into rectifying tower 1, methyl alcohol is gasified in rectifying tower 1 tower reactor.After tower top pressure reaches pressure-fired, methyl alcohol no longer enters rectifying tower 1 from vaporizer 5, changes and enters rectifying tower 1 from opening for feed 10; In operational process, monitor tower top pressure at any time, when tower top pressure is normal, industrial methanol is from opening for feed 10 charging, and when tower top pressure is not enough, industrial methanol is from methanol evaporator 5 charging.
Regulate rectifying tower 1 tower top temperature to be 63 DEG C, pressure is 0.02Mpa, and compressor A 6 compresses methanol vapor, and (compressor A inlet temperature is 63 DEG C, and intake pressure is 0.03Mpa, and temperature out is 78 DEG C, 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 flowed out bottom rectifying tower 1 tower reactor pumps into from falling-film reboiler 2 top through reboiler circulation pump 4, with the methanol vapor heat exchange after compression, the hot methanol circulation of flowing out bottom falling-film reboiler 2 enters rectifying tower 1 tower reactor, thus realizing the heating of rectifying tower 1 tower reactor methyl alcohol by the recycle methanol heat exchange in the methanol vapor of compression and falling-film reboiler 2, bottom temperature is 68 DEG C.Along with compressor A 6 load increases gradually, regulate tower top temperature, pressure qualified to refined methanol, qualified refined methanol enters receiving tank 8 after reboiler vapor liquid heat exchange.
Compressor B 7 enters gas-liquid separator 9(compressor B inlet temperature after compressing a part of methanol vapor be 62 DEG C, and intake pressure is 0.03Mpa, and temperature out is 66 DEG C, and top hole pressure is 0.08Mpa, and flow is 2400m
3/ h), gas-phase methanol after separation enters reaction tower 3 system, qualified liquid phase refined methanol enters receiving tank 8, regulate compressor B 7 load, until after two system stabilities, in reaction tower 3 tower reactor chuck, pass into steam heating makes bottom temperature reach 90 DEG C, passes into methanol gas in the alkali lye and tower that prepare and reacts (methanol feeding amount: 9m
3/ h; Alkali lye inlet amount: 1.36m
3/ h), keep stable reaction in reactive system, reaction methanol an alkali metal salt product, enters corresponding receiving tank after sampling chemical examination is qualified, and the mixed gas comprising methyl alcohol and water vapor passes into rectifying tower 1 tower reactor from reaction tower 3 tower top (temperature 78 DEG C) 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, steam flow per hour is 13.88t/h.
Embodiment 2
Solid alkali metal hydroxide (sodium hydroxide or potassium hydroxide) is joined in alkali solving can, with fresh feed pump, the methyl alcohol necessarily measured is squeezed in alkali solving can, carry out circulation and dissolve solid caustic soda, temperature in alkali solving can is controlled with recirculated water, make it temperature and remain on 50 DEG C, in alkali alcohol liquid, alkali metal hydroxide content reaches 20%, and the alkali lye forming preparation qualified is for subsequent use.
Industrial methanol (methyl alcohol 99.5%, water 0.5%, temperature 40 DEG C, flow 165kg/h) is passed into methanol evaporator 5, when liquid level reaches 90% time, 0.6Mpa, temperature 160 DEG C of saturation steam heating are passed in chuck, after heating, methyl alcohol is squeezed into rectifying tower 1, methyl alcohol is gasified in rectifying tower 1 tower reactor.After tower top pressure reaches pressure-fired, methyl alcohol no longer enters rectifying tower 1 from vaporizer 5, changes and enters rectifying tower 1 from opening for feed 10; In operational process, monitor tower top pressure at any time, when tower top pressure is normal, industrial methanol is from opening for feed 10 charging, and when tower top pressure is not enough, industrial methanol is from methanol evaporator 5 charging.
Rectifying tower 1 tower top temperature is regulated to be 60 DEG C, pressure is 0.012Mpa, compressor A 6 compresses methanol vapor, and (compressor A inlet temperature is 61 DEG C, intake pressure is 0.023Mpa, temperature out is 79 DEG C, top hole pressure is 0.67Mpa, flow is 6300m3/h), a part of methanol vapor after compression controls to pass into falling-film reboiler 2 by switch-valve A 12, the low temperature liquid phase methyl alcohol flowed out bottom rectifying tower 1 tower reactor pumps into from falling-film reboiler 2 top through reboiler circulation pump 4, with the heat exchange of compression methanol vapor, the hot methanol circulation of flowing out bottom falling-film reboiler 2 enters rectifying tower 1 tower reactor, thus realize the heating of rectifying tower 1 tower reactor methyl alcohol by the recycle methanol heat exchange in the methanol vapor of compression and falling-film reboiler 2, bottom temperature is 67 DEG C.Along with compressor A 6 load increases gradually, regulate tower top temperature, pressure qualified to refined methanol, qualified refined methanol enters receiving tank 8 after reboiler vapor liquid heat exchange.
Another part methanol vapor after compressor A 6 compresses controls to enter gas-liquid separator 9 by switch-valve B 13, gas-phase methanol after separation enters reaction tower 3 system, qualified liquid phase refined methanol enters receiving tank 8, until after two system stabilities, in reaction tower 3 tower reactor chuck, pass into steam heating makes bottom temperature reach 90 DEG C, passes into methanol gas in the alkali lye and tower that prepare and reacts (methanol feeding amount: 8.6m
3/ h; Alkali lye inlet amount: 1.46m
3/ h), keep stable reaction in reactive system, reaction methanol an alkali metal salt product, enters corresponding receiving tank after sampling chemical examination is qualified, and the mixed gas comprising methyl alcohol and water vapor passes into rectifying tower 1 tower reactor from reaction tower 3 tower top (temperature 78 DEG C) 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, steam flow per hour is 14.79t/h.
Comparative example
Adopt traditional technology
Main technologic parameters is as follows:
Rectifying tower tower top temperature is 64 DEG C, and tower top pressure is 0.015Mpa, and bottom temperature is 72 DEG C.
Reaction tower tower top temperature is 79 DEG C, and bottom temperature is 89 DEG C.
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 hydroxide is joined in alkali solving can, with fresh feed pump, the methyl alcohol necessarily measured is squeezed in alkali solving can, carry out circulation and dissolve solid caustic soda, temperature in alkali solving can is controlled with recirculated water, make it temperature and remain on 48 DEG C, in alkali alcohol liquid, alkali metal hydroxide content reaches 19%, forms the alkali lye that preparation is qualified.Industrial methanol (methyl alcohol 99.5%, water 0.5%, temperature 45 C, flow 172kg/h) passes into methanol rectifying tower tower reactor, when in tower, liquid level reaches 92% time, 0.6Mpa, temperature 160 DEG C of saturation steam heating are passed in chuck, make methyl alcohol vaporizing, open steam heating, start supplementary methyl alcohol simultaneously, make tower top discharging and keep balancing.After rectifying tower is stable, qualified anhydrous methanol is entered in reaction tower vaporizer, open steam, methyl alcohol vaporizing is allowed to enter reaction tower, and enter rectifying tower from reaction top gaseous phase pipeline, when two column distillations reach balance, start to add alkali lye from tower top, keep stable system in reaction tower, the rosaline metal salt product after sampling analysis is qualified enters corresponding receiving tank.
By statistics, adopt original technique, steam flow per hour is 18.66t/h.
Contrasted as can be seen from above three embodiments, adopt technique of the present invention, steam consumption per hour reduces more than 20% than original technique, and this absolutely proves and adopts equipment array mode of the present invention, greatly can reduce the consumption of steam, reach energy-saving and cost-reducing object.
Claims (9)
1. a production equipment for rosaline metal-salt, comprises 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 Liang Ge branch, and one of them branch is by vapour compressor A(6) be connected with reboiler (2) steam-in;
Described rectifying tower (1) tower reactor 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; Also comprise vaporizer (5), described vaporizer (5) is connected with rectifying tower (1) tower reactor.
2. a production equipment for rosaline metal-salt, comprises rectifying tower (1) and reaction tower (3), it is characterized in that:
The pipeline of described rectifying tower (1) tower top methanol steam outlet and vapour compressor A(6) 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 be divided into Liang Ge branch, 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; Also comprise vaporizer (5), described vaporizer (5) is connected with rectifying tower (1) tower reactor.
3. production equipment as claimed in claim 1 or 2, is characterized in that: described reboiler (2) is selected from the one in board-like reboiler, falling-film reboiler or shell and tube reboiler.
4. 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.
5. production equipment as claimed in claim 1 or 2, 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).
6. a production method for rosaline metal-salt, comprises the steps:
1), alkali lye is prepared with dissolve with methanol alkali metal hydroxide;
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), the Liquid Phase Methanol flowed out bottom rectifying tower (1) tower reactor is pumped into reboiler (2) by reboiler circulation pump (4) simultaneously, after Liquid Phase Methanol and methanol vapor generation heat exchange, flow out from reboiler (2) and enter tower bottom of rectifying tower;
3), another part methanol vapor of tower top is through compressor B(7) 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, from reaction tower (3) top charging, reacts with the methanol vapor risen from tower reactor, and the rosaline metal-salt obtained is from discharging at the bottom of reaction tower (3) tower.
7. a production method for rosaline metal-salt, comprises the steps:
1), alkali lye is prepared with dissolve with methanol alkali metal hydroxide;
2), industrial methanol is vaporized in rectifying tower (1) tower reactor; The methanol vapor of tower top is through compressor A(6) compress rear portion methanol vapor and pass into reboiler (2), the Liquid Phase Methanol flowed out bottom rectifying tower (1) tower reactor is pumped into reboiler (2) by reboiler circulation pump (4) simultaneously, after Liquid Phase Methanol and methanol vapor generation heat exchange, flow out from reboiler (2) 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, from the charging of reaction tower top, reacts with the methanol vapor risen from tower reactor, and the rosaline metal-salt obtained is from discharging at the bottom of reaction tower (3) tower.
8. production method as claimed in claims 6 or 7, is characterized in that: described reboiler (2) is selected from: the one in board-like reboiler, falling-film reboiler or shell and tube reboiler.
9. production method as claimed in claims 6 or 7, is characterized in that: the gas of reaction tower (3) tower top output passes into rectifying tower (1) tower reactor through piping 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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| CN201310352913.5A CN103387483B (en) | 2013-08-14 | 2013-08-14 | Production device and process of methanol alkali metal salts |
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| CN201310352913.5A CN103387483B (en) | 2013-08-14 | 2013-08-14 | Production device and process of methanol alkali metal salts |
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| CN103387483B true CN103387483B (en) | 2015-06-17 |
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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 |
| 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 |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1333202A (en) * | 2000-06-09 | 2002-01-30 | 克拉里安特国际有限公司 | Preparation for alcohol solution of alkali metal alcohol salt |
| CN1409696A (en) * | 1999-12-08 | 2003-04-09 | 巴斯福股份公司 | Method for producing alkali methylates |
| CN1626488A (en) * | 2004-08-13 | 2005-06-15 | 于志波 | Technique of alkaline process for producing sodium methoxide/sodium ethylate |
| 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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- 2013-08-14 CN CN201310352913.5A patent/CN103387483B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1409696A (en) * | 1999-12-08 | 2003-04-09 | 巴斯福股份公司 | Method for producing alkali methylates |
| CN1333202A (en) * | 2000-06-09 | 2002-01-30 | 克拉里安特国际有限公司 | Preparation for alcohol solution of alkali metal alcohol salt |
| CN1626488A (en) * | 2004-08-13 | 2005-06-15 | 于志波 | Technique of alkaline process for producing sodium methoxide/sodium ethylate |
| 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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