CN101613289A - The abbreviated system that thanomin is produced - Google Patents
The abbreviated system that thanomin is produced Download PDFInfo
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- CN101613289A CN101613289A CN200910098497A CN200910098497A CN101613289A CN 101613289 A CN101613289 A CN 101613289A CN 200910098497 A CN200910098497 A CN 200910098497A CN 200910098497 A CN200910098497 A CN 200910098497A CN 101613289 A CN101613289 A CN 101613289A
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- pump
- oxyethane
- thanomin
- liquefied ammonia
- stable
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Abstract
The present invention relates to liquefied ammonia (NH
3) and oxyethane (EO) make raw material, in the presence of the less water catalyzer, produce the abbreviated system of thanomin.Abbreviated system of the present invention, be by round-robin Monoethanolamine MEA BASF (MEA) or diethanolamine (DEA) measure accurately to the liquefied ammonia that drops into reaction, oxyethane, water catalyzer and in order to adjust the product ratio, many operating parameterss such as the flow in the production process, temperature, pressure (pressure reduction), liquid level are controlled automatically, make reaction product component keep the stable operation of temperature and rectifying separation system to realize, whole flow process has reduced middle-chain, make plant construction to reduce investment outlay, can save process cost in process of production.
Description
Technical field
The invention belongs to the thanomin preparation field, specifically, relate to a kind of with liquefied ammonia (NH
3) and oxyethane (EO) make raw material, in the presence of the less water catalyzer, produce the abbreviated system of thanomin.
Technical background
The reaction of ammonia and oxyethane is reaction successively, can generate three kinds of products simultaneously:
NH
3+C
2H
4O→H
2NC
2H
4OH MEA
H
2NC
2H
4OH+C
2H
4O→HN(C
2H
4OH)
2 DEA
HN(C
2H
4OH)
2+C
2H
4O→HN(C
2H
4OH)
3 TEA
Modern Large Scale and Continuous thanomin production technique has two types usually:
A kind of is " dry method ", and promptly liquefied ammonia adds less water as catalyzer with after oxyethane mixes, and under higher temperature and pressure, reacts in pipeline reactor, and product is through deamination, dehydration, and last rectifying separation goes out three kinds of thanomin products.(see figure 1) is in this flow process, and D-201 is tundish, the intermediates that the device that its volume was enough to store 4 hours is produced.
Another kind is " wet method " technology, is about to ammonia and is configured to 20-50% ammoniacal liquor, mixes with oxyethane again, reacts in the pipeline piston flow reactor, and product is through deamination, dehydration, drying, and last rectifying separation goes out three kinds of thanomin products.(see figure 2) in this flow process polygamy system ammonia absorber T-101,1-2 platform dehydration tower T-202, (T-203) and intermediates jar D-203, two equipment such as interchanger E-206, E-207.The intermediates that the device that the volume of intermediates jar was enough to store a day is produced.
In two kinds of technical process, " wet method " flow process is simple for " dry method " flow process, and investment cost is low, and energy consumption is few, and process cost is low.Therefore, the present invention adopts " dry method " production technique, saves the product tundish, and flow process connects, and can further reduce investment outlay and energy efficient and process cost.
Summary of the invention
The abbreviated system that thanomin of the present invention is produced, be to be raw material with liquefied ammonia, oxyethane, the water that adds the 2-10% that drops into the liquefied ammonia amount is as catalyzer, and reactant is after deamination, dehydration, directly enter the rectifying separation system, obtain MEA, DEA, three kinds of products of TEA at last.The intermediates jar is not set.(see figure 3)
Thanomin abbreviated system of the present invention, matter of utmost importance are will guarantee reaction product component stable.For this purpose, the present invention at first takes the starting material to dropping into---and liquefied ammonia, oxyethane and water catalyzer, round-robin Monoethanolamine MEA BASF or diethanolamine carry out strict metering.P-101 oxyethane charging pump is selected METERING DIAPHRAGM PUMPS or ram pump for use among Fig. 3, and P-102 liquefied ammonia charging pump is selected three plunger high pressure reciprocating pumps for use, and P-103 water catalyst pump is selected ram pump for use, and P-104 Monoethanolamine MEA BASF recycle pump is also selected ram pump for use.Above-mentioned all pumps all adopt variable frequency adjustment, can accurately calculate the quantity that enters each section reactor feed liquid.Inlet amount accurately, guaranteed that the reaction product component is stable.
Thanomin abbreviated system of the present invention, second kind of means is to take into full account turndown ratio in the equipment design, device can carry out normal running under the 40-110% load.
Thanomin production abbreviated system of the present invention, the third means are to adopt distributed control system (DCS), uninterrupted (UPS) power supply of outfit, and the flow in the production process, temperature, pressure (pressure reduction), liquid level control are automatic operation.The hazardous location is provided with detector, has automatic warning function, thereby guarantees the normal and safe operation of complete assembly.
50kt/a thanomin production abbreviated system of the present invention compares with " wet method " technology, has saved ammonia absorber (T-101), at least one dehydration tower (T-201), two interchanger (E-206, E-207), a product relay tank (D-203).Compare with " dry method " technology (Fig. 1), saved product tundish D-201 and residual ammonia absorber (T-201) and desorption tower (T-202).Simultaneously, thanomin production abbreviated system of the present invention can meet or exceed the productive rate and the quality product of existing dry process same device.For example: the oxyethane utilization ratio reaches more than 99%, and the ammonia utilization ratio reaches more than 98%, and product yield reaches more than 98.5%, and ton product steam consumption is below 2.5 tons.Therefore, technology of the present invention can be saved the energy consumption in construction investment and the production process significantly, and working cost reduces has saved production cost.
Description of drawings
Fig. 1 dry process schema of the prior art;
Among Fig. 1: D-101---catalyst tank; R-101/A/B/C/D/E/F---reactor; T-101---ammonia still; T-201---deammoniation tower; D-201---non-conservation tank; T-202---ammonia desorption tower; T-301---drying tower; T-302---Monoethanolamine MEA BASF rectifying tower; T-303---diethanolamine, trolamine rectifying tower; V-301/302/303---vacuum system; D-301/302/303/304---product non-conservation tank.
Fig. 2 wet processing schema of the prior art;
Among Fig. 2: T-101---ammonia absorber; MX-101---static mixer; R-101---reactor; T-201---deammoniation tower; T-202---dehydration tower; D-203---product tundish; T-301---drying tower; T-302---MEA rectifying tower; T-303---DEA rectifying tower; T-304---TEA rectifying tower; D-301/302/303/304---product non-conservation tank;
The abbreviated system schema of Fig. 3 thanomin of the present invention.
Among Fig. 3: D-101---the EO storage tank; D-102---liquid ammonia storage tank; P-101---EO charging pump; P-102---liquefied ammonia charging pump; P-104---catalyst pump; P-105---water is towards pump; R-101---reactor; T-101---ammonia still; D-103---catalyst tank; E-101---reboiler; E-102/103---ammonia condenser; FB-101---flash tank; E-104/105/106---condenser; T-102---dehydration tower; T-201---MEA rectifying tower; T-202---DEA rectifying tower; T-203---TEA rectifying tower; E-201/205/209---reboiler; J-201/202---vacuum pump; E-202/206/210---condenser; D-201/202/203/204---product non-conservation tank.
Embodiment:
Abbreviated system operational load of the present invention is relatively stable, reaction product product ratio MEA: DEA: TEA=3: 4: 3.
1. dehydration tower (T-102) operational condition control: tower top pressure 25Kpa, 65 ℃ of tower top temperatures, 145-150 ℃ of tower still temperature, surplus water content is below 0.3% in the reaction product.
2. Monoethanolamine MEA BASF rectifying tower (T-201) feed composition is stable, feeding temperature 115-120 ℃, the control tower operational condition: tower top pressure 2.0Kpa, 78 ℃ of tower top temperatures, 165-170 ℃ of tower still temperature, reflux ratio 0.3, tower operate steadily, and rectifying obtains the Monoethanolamine MEA BASF product more than 99.5%.
Although above the specific embodiment of the present invention has been given to describe in detail and explanation; but should indicatedly be; we can carry out various equivalences to above-mentioned embodiment according to conception of the present invention and change and modification; when the function that it produced does not exceed spiritual that specification sheets and accompanying drawing contain yet, all should be within protection scope of the present invention.
Claims (4)
1, a kind of abbreviated system of producing thanomin, to starting material liquefied ammonia, oxyethane, water catalyzer, the round-robin MEA that enters reactor, DEA all adopts the volume pump of relevant pressure, flow, the flow variable ratio frequency changer is regulated, it is characterized in that the oxyethane charging pump selects METERING DIAPHRAGM PUMPS or ram pump for use, the liquefied ammonia charging pump is selected three plunger high pressure reciprocating pumps for use, the water catalyst pump is selected ram pump for use, the Monoethanolamine MEA BASF recycle pump is selected ram pump for use, described all pumps all adopt variable frequency adjustment, make the reaction product component stable, guarantee the stable operation of rectifying separation system.
2,, the intermediates storage tank is not set wherein according to the described technology of claim 1.
3, technology according to claim 2, wherein operation of equipment is stable can normal running under the 40-110% load.
4, method according to claim 1 wherein adopts distributed control system, and mass flow, temperature, pressure, liquid level control are automatic operation, and the hazardous location is provided with assurance device at the stable detector of slave mode.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910098497A CN101613289A (en) | 2009-05-12 | 2009-05-12 | The abbreviated system that thanomin is produced |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910098497A CN101613289A (en) | 2009-05-12 | 2009-05-12 | The abbreviated system that thanomin is produced |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101613289A true CN101613289A (en) | 2009-12-30 |
Family
ID=41493200
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|---|---|---|---|
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102357351A (en) * | 2011-07-27 | 2012-02-22 | 湖北仙粼化工有限公司 | Direct reflux reaction apparatus for high pressure reaction materials used for production of ethanolamine |
| CN103271238A (en) * | 2013-05-10 | 2013-09-04 | 中国科学院亚热带农业生态研究所 | Preparation method of feed additive mono ethanol amine and application |
| CN103623674A (en) * | 2013-12-06 | 2014-03-12 | 佳化化学（滨州）有限公司 | Absorbent absorbing gas containing epoxide |
| CN106608829A (en) * | 2015-10-22 | 2017-05-03 | 中国石油化工股份有限公司 | Ammonia recovery method in ethanolamine combined production technology |
| CN106608834A (en) * | 2015-10-22 | 2017-05-03 | 中国石油化工股份有限公司 | Method for cooperatively producing ethanolamine through liquid ammonia method and ammonium hydroxide method |
| CN106608831A (en) * | 2015-10-22 | 2017-05-03 | 中国石油化工股份有限公司 | Recycling method of ammonia in ethanol amine combined production |
| CN106608832A (en) * | 2015-10-22 | 2017-05-03 | 中国石油化工股份有限公司 | Technological method for cooperatively producing ethanolamine through liquid ammonia method and ammonium hydroxide method |
| CN107943161A (en) * | 2017-09-27 | 2018-04-20 | 天津大学 | The control method of reactive distillation film device coupling process |
| CN106608830B (en) * | 2015-10-22 | 2018-06-08 | 中国石油化工股份有限公司 | Ammonia Process and liquid ammonia process for caustic soda purification Joint Production ethanol amine method |
| CN106608833B (en) * | 2015-10-22 | 2018-07-13 | 中国石油化工股份有限公司 | Ethanol amine co-production |
| CN112961062A (en) * | 2014-04-04 | 2021-06-15 | 沙特基础工业全球技术有限公司 | Minimizing water content in ethanolamine product streams |
-
2009
- 2009-05-12 CN CN200910098497A patent/CN101613289A/en active Pending
Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102357351A (en) * | 2011-07-27 | 2012-02-22 | 湖北仙粼化工有限公司 | Direct reflux reaction apparatus for high pressure reaction materials used for production of ethanolamine |
| CN102357351B (en) * | 2011-07-27 | 2014-07-23 | 湖北仙粼化工有限公司 | Direct reflux reaction apparatus for high pressure reaction materials used for production of ethanolamine |
| CN103271238A (en) * | 2013-05-10 | 2013-09-04 | 中国科学院亚热带农业生态研究所 | Preparation method of feed additive mono ethanol amine and application |
| CN103271238B (en) * | 2013-05-10 | 2014-04-02 | 中国科学院亚热带农业生态研究所 | Preparation method of feed additive mono ethanol amine and application |
| CN103623674A (en) * | 2013-12-06 | 2014-03-12 | 佳化化学（滨州）有限公司 | Absorbent absorbing gas containing epoxide |
| CN112961062A (en) * | 2014-04-04 | 2021-06-15 | 沙特基础工业全球技术有限公司 | Minimizing water content in ethanolamine product streams |
| CN106608832A (en) * | 2015-10-22 | 2017-05-03 | 中国石油化工股份有限公司 | Technological method for cooperatively producing ethanolamine through liquid ammonia method and ammonium hydroxide method |
| CN106608831A (en) * | 2015-10-22 | 2017-05-03 | 中国石油化工股份有限公司 | Recycling method of ammonia in ethanol amine combined production |
| CN106608834A (en) * | 2015-10-22 | 2017-05-03 | 中国石油化工股份有限公司 | Method for cooperatively producing ethanolamine through liquid ammonia method and ammonium hydroxide method |
| CN106608830B (en) * | 2015-10-22 | 2018-06-08 | 中国石油化工股份有限公司 | Ammonia Process and liquid ammonia process for caustic soda purification Joint Production ethanol amine method |
| CN106608833B (en) * | 2015-10-22 | 2018-07-13 | 中国石油化工股份有限公司 | Ethanol amine co-production |
| CN106608829B (en) * | 2015-10-22 | 2018-07-17 | 中国石油化工股份有限公司 | Ammonia recovery method in ethanol amine joint production process |
| CN106608834B (en) * | 2015-10-22 | 2018-10-23 | 中国石油化工股份有限公司 | The method of liquid ammonia process for caustic soda purification and Ammonia Process co-producing ethanol amine |
| CN106608832B (en) * | 2015-10-22 | 2018-10-23 | 中国石油化工股份有限公司 | The process of liquid ammonia process for caustic soda purification and Ammonia Process co-producing ethanol amine |
| CN106608831B (en) * | 2015-10-22 | 2019-04-12 | 中国石油化工股份有限公司 | The recovery method of ammonia in ethanol amine joint production process |
| CN106608829A (en) * | 2015-10-22 | 2017-05-03 | 中国石油化工股份有限公司 | Ammonia recovery method in ethanolamine combined production technology |
| CN107943161A (en) * | 2017-09-27 | 2018-04-20 | 天津大学 | The control method of reactive distillation film device coupling process |
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Application publication date: 20091230 |