CN114276255A - Ethanolamine multi-section tubular reaction energy-saving production system and production process - Google Patents
Ethanolamine multi-section tubular reaction energy-saving production system and production process Download PDFInfo
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- CN114276255A CN114276255A CN202111549470.XA CN202111549470A CN114276255A CN 114276255 A CN114276255 A CN 114276255A CN 202111549470 A CN202111549470 A CN 202111549470A CN 114276255 A CN114276255 A CN 114276255A
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- ammonia
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- ethanolamine
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- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 title claims abstract description 157
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 55
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 24
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 249
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 109
- 238000000926 separation method Methods 0.000 claims abstract description 84
- 239000012528 membrane Substances 0.000 claims abstract description 82
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 58
- IAYPIBMASNFSPL-UHFFFAOYSA-N Ethylene oxide Chemical compound C1CO1 IAYPIBMASNFSPL-UHFFFAOYSA-N 0.000 claims abstract description 37
- 239000000463 material Substances 0.000 claims abstract description 21
- 239000007788 liquid Substances 0.000 claims description 88
- 238000000034 method Methods 0.000 claims description 15
- 230000001105 regulatory effect Effects 0.000 claims description 11
- 230000001276 controlling effect Effects 0.000 claims description 7
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 abstract description 22
- GSEJCLTVZPLZKY-UHFFFAOYSA-N Triethanolamine Chemical compound OCCN(CCO)CCO GSEJCLTVZPLZKY-UHFFFAOYSA-N 0.000 abstract description 19
- 239000012535 impurity Substances 0.000 abstract description 4
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 abstract description 2
- 230000002195 synergetic effect Effects 0.000 abstract description 2
- 229940031098 ethanolamine Drugs 0.000 description 45
- 239000000047 product Substances 0.000 description 15
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 238000005086 pumping Methods 0.000 description 5
- 238000007259 addition reaction Methods 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 238000004821 distillation Methods 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 238000001223 reverse osmosis Methods 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
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- Separation Using Semi-Permeable Membranes (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to an ethanolamine production process, in particular to an ethanolamine multi-section tubular reaction energy-saving production system and a production process. The membrane separation assembly is provided with the booster pump behind, and the pressure difference required by membrane separation is provided by the synergistic action of the pressure of the reaction materials and the booster pump. After each stage of reaction, most of water and liquid ammonia are separated from ethanolamine (monoethanolamine, diethanolamine and triethanolamine) in time, so that water and ammonia with less ethanolamine content participate in the next stage of reaction after being pressurized by a pump, thereby reducing the reaction chance of the monoethanolamine, diethanolamine and triethanolamine with ethylene oxide and reducing reaction impurities.
Description
Technical Field
The invention relates to an ethanolamine production process, in particular to an ethanolamine multi-section tubular reaction energy-saving production system and a production process.
Background
Monoethanolamine (MEA), Diethanolamine (DEA), and Triethanolamine (TEA) are collectively referred to as ethanolamine, and ethanolamine is obtained by the reaction of ethylene oxide and ammonia under water catalysis to produce Monoethanolamine (MEA), Diethanolamine (DEA), and Triethanolamine (TEA), which are consecutive addition reactions. Ammonia (NH)3) And Ethylene Oxide (EO) above ambient temperature, gaseous or liquid, in small amounts, such as water, or the products EA of the reaction itself (of MEA, DEA, TEA)Collectively called) as a catalyst, can accelerate the addition reaction to generate monoethanolamine MEA; the MEA and the EO continue to perform addition reaction to generate diethanolamine DEA; DEA also proceeds with addition reaction with EO to form triethanolamine TEA.
The chemical reaction equation of ethanolamine is as follows:
the molar ratio of the existing liquid ammonia to the epoxy ethane is usually 3.5-10, excessive liquid ammonia needs to be distilled out of reaction materials after reaction, and the consumption of steam for distillation and separation is high.
Disclosure of Invention
The invention aims to: through the ethanol amine multi-section tubular reaction energy-saving production system, the rough separation of water, liquid ammonia and ethanol amine is realized, the steam consumption of separating water and ammonia by a rectification mode after a reactor is reduced, and the energy consumption of unit products is reduced. Meanwhile, the reaction chance of ethylene oxide with monoethanolamine and diethanolamine can be reduced, the proportion of monoethanolamine in ethanolamine products is greatly improved, the proportion of diethanolamine and triethanolamine is correspondingly reduced, and the adjustment of the proportion of each component in the products is facilitated, so that the product is more suitable for the market demand. When the demand of the market for the monoethanolamine is reduced, the membrane module is stopped, and even the monoethanolamine and the diethanolamine are returned to the reactor, so that the proportion of the diethanolamine and the triethanolamine is increased.
The technical scheme of the invention is as follows: an ethanolamine multi-section tubular reaction energy-saving production system comprises a pipeline mixer, and is characterized in that a liquid ammonia pipe, a circulating ammonia pipe and an ethylene oxide pipe are respectively connected with a first pipeline mixer through a mass flow meter, the first pipeline mixer is connected with the first tubular reactor, the first tubular reactor is connected with a first membrane separation component, the clear liquid end of the first membrane separation component is connected with a first circulating ammonia liquid pressure pump, the first circulating ammonia liquid pressure pump is connected with a second pipeline mixer, the second pipeline mixer is connected with a second tubular reactor, the second tubular reactor is connected with a second membrane separation component, the clear liquid end of the second membrane separation component is connected with a second circulating ammonia liquid pressure pump, the second circulating ammonia liquid pressure pump is connected with a third pipeline mixer, the third pipeline mixer is connected with a third tubular reactor, and the third tubular reactor is connected with a third membrane separation component, the clear liquid end of the third membrane separation component is connected with a third circulating ammonia liquid pressurizing pump, the third circulating ammonia liquid pressurizing pump is connected with the circulating ammonia liquid pipe, and the concentrated liquid end of the first membrane separation component, the concentrated liquid end of the second membrane separation component and the concentrated liquid end of the third membrane separation component are connected in parallel and then output.
And a mass flow meter is connected between the first circulating ammonia liquid pressurizing pump and the second pipeline mixer. And a mass flow meter is connected between the second circulating ammonia liquid pressurizing pump and the third pipeline mixer.
The second pipeline mixer and the third pipeline mixer are also connected with an ethylene oxide pipe.
A production process of an ethanolamine multi-section tubular reaction energy-saving production device comprises the following steps: step one, continuously metering liquid ammonia, circulating ammonia liquid and ethylene oxide by a mass flow meter, then feeding the liquid ammonia, the circulating ammonia liquid and the ethylene oxide into a high-efficiency pipeline mixer, then feeding the liquid ammonia, the circulating ammonia liquid and the ethylene oxide into a first tubular reactor for reaction, controlling the temperature of materials at 45-60 ℃ after the first-stage reaction is finished, feeding the materials into a first membrane separation assembly, allowing ammonia, water and a small amount of ethanolamine to flow out of a clear liquid end of the first membrane separation assembly, allowing the rest ammonia, water and ethanolamine to flow out of a concentrated liquid end of the membrane separation assembly, and feeding the ammonia, water and ethanolamine to an ammonia still in the next process after passing through a pressure regulating valve and the mass flow meter;
step two, ammonia, water and a small amount of ethanolamine flow out of a clear liquid end of a first membrane separation component D, are pressurized by a first booster pump, enter a second pipeline mixer and then enter a first tubular reactor for reaction, after the second-stage reaction is finished, the temperature of the material is controlled to be 45-60 ℃, and then enter a second membrane separation component, the ammonia, the water and the small amount of ethanolamine flow out of a clear liquid end of the second membrane separation component, the rest ammonia, the water and the ethanolamine flow out of a concentrated liquid end of the membrane separation component, and the ammonia, the water and the ethanolamine flow out of an ammonia still tower in the next process after passing through a pressure regulating valve and a mass flow meter;
and step three, allowing ammonia, water and a smaller amount of ethanolamine to flow out of a clear liquid end of the second membrane separation assembly D, pressurizing by a second booster pump, allowing the ammonia, the water and the smaller amount of ethanolamine to enter a third pipeline mixer, allowing the ammonia, the water and the smaller amount of ethanolamine to enter a third tubular reactor for reaction, controlling the temperature of the material to be 45-60 ℃ after the third stage of reaction is finished, allowing the material to enter a third membrane separation assembly, allowing ammonia liquid to flow out of a clear liquid end of the third membrane separation assembly, pressurizing by a third booster pump, and allowing the ammonia liquid to enter a circulating ammonia liquid pipe to participate in system circulation. The rest ammonia, water and ethanolamine flow out from the concentrated solution end of the membrane separation component D, pass through a pressure regulating valve and a mass flow meter and then go to an ammonia still in the next procedure.
According to the invention, the reverse osmosis membrane separation component is additionally arranged behind the multi-section tubular reactor, so that the rough separation of water, liquid ammonia and ethanolamine can be realized, the steam consumption for separating water and ammonia by a rectification mode behind the reactor is reduced, and the energy consumption of unit products is reduced. In the production process, all or part of the reverse osmosis membrane separation components can be started, and the reverse osmosis membrane separation components can also not be started. When the membrane separation component is used, compared with the existing multi-section tubular reactor, the proportion of monoethanolamine in the ethanolamine product is greatly improved, and the proportion of diethanolamine and triethanolamine is correspondingly reduced. The proportion of each component in the product can be conveniently adjusted according to the market demand on monoethanolamine, diethanolamine and triethanolamine.
Whether the product structure is adjusted or not, the membrane module behind the end reactor is started, so that the water and the liquid ammonia are roughly separated from the reaction product and returned to the first inlet of the reactor, and the energy consumption of the product is reduced.
The membrane separation assembly is provided with the booster pump behind, and the pressure difference required by membrane separation is provided by the synergistic action of the pressure of the reaction materials and the booster pump. After each stage of reaction, most of water and liquid ammonia are separated from ethanolamine (monoethanolamine, diethanolamine and triethanolamine) in time, so that water and ammonia with less ethanolamine content participate in the next stage of reaction after being pressurized by a pump, thereby reducing the reaction chance of the monoethanolamine, diethanolamine and triethanolamine with ethylene oxide and reducing reaction impurities.
The molar ratio of each section of feed of the invention is liquid ammonia: the ethylene oxide is more than or equal to 10, the polymerization hazard of the ethylene oxide is avoided, the side reaction is reduced, the impurities generated by the reaction are less, and the content of the monoethanolamine in the product can reach 60%.
According to the invention, the membrane separation component secondary line is arranged behind each section of reactor, and reaction materials can directly go to the next section of reactor through the secondary line without passing through a membrane component and a booster pump, so that process adjustment and maintenance are facilitated.
Compared with the prior art, the invention has the following advantages:
1. the process provided by the invention provides an energy-saving process method for producing ethanolamine, and solves the problem that a large amount of ammonia needs to be distilled, separated and recycled after reaction, so that the energy consumption is high.
2. The process can also greatly improve the proportion of the monoethanolamine in the product, and is convenient for adjusting the structure of the product. Compared with the prior multi-section tubular reactor, the reactor can more flexibly adjust the product proportion of the monoethanolamine, the diethanolamine and the triethanolamine, and is suitable for the market demand.
3. Install the membrane separation subassembly additional behind every section reactor, the ammonia that will need go on behind the reactor, separation of water is gone on behind every section reactor in advance, has reduced the steam consumption of rectification separation behind the reactor, and product composition proportion adjusts more nimble convenience simultaneously, and impurity reduces.
Drawings
FIG. 1 is a schematic diagram of the system and process of the present invention.
In the figure: 1-water mass flowmeter, 2-liquid ammonia mass flowmeter, 3-circulating ammonia liquid mass flowmeter, 4-ethylene oxide flowmeter, 5-mixed ethanolamine flowmeter, 5-pressure regulating valve, A-pipeline mixer, B-pipeline reactor, C-circulating ammonia liquid pressure pump, D-membrane separation assembly, 11-water pipe, 12-liquid ammonia pipe, 13-circulating ammonia liquid pipe and 15-ethylene oxide pipe.
Detailed Description
The invention is further illustrated by the following specific examples:
the ethanolamine multi-section tubular reaction energy-saving production system comprises a pipeline mixer, and is characterized in that a water pipe 11, a liquid ammonia pipe 12, a circulating ammonia pipe 13 and an ethylene oxide pipe 15 are respectively connected with a first pipeline mixer A1 through mass flow meters (1, 2, 3 and 4), the first pipeline mixer A1 is connected with a first tubular reactor B1, the first tubular reactor B1 is connected with a first membrane separation component D1, the clear liquid end of the first membrane separation component D1 is connected with a first circulating ammonia liquid pressurizing pump C1, the first circulating ammonia liquid pressurizing pump C1 is connected with a second pipeline mixer A2, a second pipeline mixer A2 is connected with a second tubular reactor B2, the second tubular reactor is connected with a second membrane separation component D2, the clear liquid end of the second membrane separation component is connected with a second circulating ammonia liquid pressurizing pump C2, and the second circulating ammonia liquid pressurizing pump C2 is connected with a third pipeline mixer A3, the third pipeline mixer A3 is connected with a third pipeline reactor B3, the third pipeline reactor is connected with a third membrane separation module D3, the clear liquid end of the third membrane separation module is connected with a third circulating ammonia liquid pressure pump C3, the third circulating ammonia liquid pressure pump C3 is connected with the circulating ammonia liquid pipe 13, and the concentrated liquid end of the first membrane separation module D1, the concentrated liquid end of the second membrane separation module D2 and the concentrated liquid end of the third membrane separation module D3 are connected in parallel through a pressure regulating valve 6 and a mass flow meter 5 and then output.
And a mass flow meter 3 is connected between the first circulating ammonia liquid pressurizing pump C1 and the second pipeline mixer A2. And a mass flow meter 3 is connected between the second circulating ammonia liquid pressurizing pump C2 and the third pipeline mixer A3. The second pipeline mixer and the third pipeline mixer are also respectively connected with an ethylene oxide pipe 4.
After the system is installed, the pressure is tested by water, the residual water in the reaction process equipment can be drained when the pressure is tested to be qualified by water pressure, then the airtightness is checked, the nitrogen is swept and replaced until the content of the exhaust port sample is consistent with that of the nitrogen sample at the inlet, and then the nitrogen discharge valve and the air inlet valve at each position are closed. And (3) communicating the whole reaction section, starting a liquid ammonia pump to inject liquid ammonia from an inlet of the first section of the reactor, slowly increasing the pressure of the reaction section to 6.0-7.0 MPa, filling the reactor with the liquid ammonia, then performing an ammonia distillation process, and circularly returning the liquid ammonia to the inlet of the liquid ammonia pump by distilling the liquid ammonia through an ammonia distillation tower to form a liquid ammonia large circulation. While the liquid ammonia is largely circulated, the reactor jacket is heated with hot water until the temperature required for the reaction is reached. Then respectively starting a catalyst pump (water pump), an ethylene oxide pump and the like, and pumping materials such as water, ethylene oxide and the like into the reactor according to the specified flow.
The complete production process comprises the following steps:
step one, continuously metering liquid ammonia, circulating ammonia liquid and ethylene oxide through mass flow meters 1, 2, 3 and 4 respectively, then feeding the liquid ammonia, the circulating ammonia liquid and the ethylene oxide into a high-efficiency pipeline mixer A1, then feeding the liquid ammonia, the circulating ammonia liquid and the ethylene oxide into a first tubular reactor B1 for reaction, controlling the temperature of materials at 45-60 ℃ after the first-stage reaction is finished, feeding the materials into a first membrane separation component D1, allowing ammonia, water and a small amount of ethanolamine to flow out of a clear liquid end of the first membrane separation component D1, allowing the rest ammonia, water and ethanolamine to flow out of a concentrated liquid end of the membrane separation component D1, and feeding the rest ammonia, water and ethanolamine into an ammonia still in the next process after passing through a pressure regulating valve 6 and a mass flow meter 5;
step two, enabling ammonia, water and a small amount of ethanolamine to flow out of a clear liquid end of a first membrane separation component D, pressurizing by a first booster pump C1, enabling the ammonia, the water and the small amount of ethanolamine to enter a second pipeline mixer A2, enabling the ammonia, the water and the small amount of ethanolamine to enter a first tubular reactor B2 for reaction, controlling the temperature of materials to be 45-60 ℃ after the second-stage reaction is finished, enabling the materials to enter a second membrane separation component D2, enabling the ammonia, the water and the small amount of ethanolamine to flow out of a clear liquid end of the second membrane separation component D2, enabling the rest ammonia, the water and the ethanolamine to flow out of a concentrated liquid end of a membrane separation component D2, and enabling the rest ammonia, the water and the ethanolamine to flow out of an ammonia still for the next process after passing through a pressure regulating valve and a mass flow meter 5;
and step three, allowing ammonia, water and a smaller amount of ethanolamine to flow out of a clear liquid end of a second membrane separation assembly D, pressurizing by a second booster pump C2, allowing the ammonia, the water and the smaller amount of ethanolamine to enter a third pipeline mixer A3, allowing the ammonia, the smaller amount of ethanolamine to enter a third tubular reactor B3 for reaction, controlling the temperature of materials to be 45-60 ℃ after the third-stage reaction is finished, allowing the materials to enter a third membrane separation assembly D3, allowing ammonia liquid to flow out of a clear liquid end of a third membrane separation assembly D3, pressurizing by a third booster pump C3, and allowing the ammonia liquid to enter a circulating ammonia liquid pipe to participate in system circulation. The rest ammonia, water and ethanolamine flow out of the concentrated solution end of the membrane separation component D, pass through a pressure regulating valve and a mass flowmeter 5 and then enter an ammonia still in the next procedure; the post-treatment process is conventional technology and flow, and is not described herein. The following embodiments are respectively implemented on the basis of the above.
Example 1:
pumping liquid ammonia 7.44 t/h (containing recycled ammonia of membrane separation after reaction 4 t/h), water 0.38 t/h and ethylene oxide 0.9 t/h into a first inlet of the reactor; the second inlet pumps ethylene oxide for 0.8 t/h; the third inlet pumps ethylene oxide for 0.8 t/h; only the third membrane separation component is started, and the ammonia is recycled for 4t/h through membrane separation, so that the steam consumption can be saved by 2.5 t/h. The output of the ethanolamine is 3.20t/h, wherein the content of the monoethanolamine, the diethanolamine and the triethanolamine is 55%, 30% and 15%.
Example 2:
pumping liquid ammonia 7.42 t/h, water 0.38 t/h and ethylene oxide 1.2 t/h into a first inlet of the reactor, and starting a membrane separation assembly behind the first section of the reactor; pumping ethylene oxide into the second inlet for 0.8 t/h, and starting a membrane separation assembly behind the second reactor; the third inlet pumps ethylene oxide for 0.5 t/h; and the third membrane separation assembly is not started, so that the steam consumption is not saved. The output of the ethanolamine is 3.26t/h, wherein the proportion of monoethanolamine, diethanolamine and triethanolamine is 65%, 26% and 9%, and the proportion of monoethanolamine is increased.
Example 3:
pumping liquid ammonia 3.4 t/h (containing recycled ammonia 1.5 t/h), water 0.2 t/h and ethylene oxide 0.9 t/h into a first inlet of the reactor; the second inlet pumps ethylene oxide for 0.8 t/h; the third inlet pumps ethylene oxide for 0.8 t/h; only the third membrane separation component is started, and the ammonia is recycled by 1.5t/h through membrane separation, so that the steam consumption can be saved by 1 t/h. The output of the ethanolamine is 3.10t/h, wherein the content of the monoethanolamine, the diethanolamine and the triethanolamine is 38%, 37% and 25%.
Claims (5)
1. An ethanolamine multi-section tubular reaction energy-saving production system comprises a pipeline mixer, and is characterized in that a liquid ammonia pipe, a circulating ammonia pipe and an ethylene oxide pipe are respectively connected with a first pipeline mixer through a mass flow meter, the first pipeline mixer is connected with the first tubular reactor, the first tubular reactor is connected with a first membrane separation component, the clear liquid end of the first membrane separation component is connected with a first circulating ammonia liquid pressure pump, the first circulating ammonia liquid pressure pump is connected with a second pipeline mixer, the second pipeline mixer is connected with a second tubular reactor, the second tubular reactor is connected with a second membrane separation component, the clear liquid end of the second membrane separation component is connected with a second circulating ammonia liquid pressure pump, the second circulating ammonia liquid pressure pump is connected with a third pipeline mixer, the third pipeline mixer is connected with a third tubular reactor, and the third tubular reactor is connected with a third membrane separation component, the clear liquid end of the third membrane separation component is connected with a third circulating ammonia liquid pressurizing pump, the third circulating ammonia liquid pressurizing pump is connected with the circulating ammonia liquid pipe, and the concentrated liquid end of the first membrane separation component, the concentrated liquid end of the second membrane separation component and the concentrated liquid end of the third membrane separation component are connected in parallel and then output.
2. The energy-saving production system for the multistage tubular reaction of ethanolamine according to claim 1, wherein a mass flow meter is connected between the first circulating ammonia liquid pressurizing pump and the second pipeline mixer.
3. The energy-saving production system for the multistage tubular reaction of ethanolamine according to claim 1, wherein a mass flow meter is connected between the second circulating ammonia liquid pressurizing pump and the third pipeline mixer.
4. The energy-saving production system for multistage tubular reaction of ethanolamine according to claim 1, wherein the second pipeline mixer and the third pipeline mixer are further connected with an ethylene oxide pipe.
5. A production process adopting the ethanolamine multistage tubular reaction energy-saving production device disclosed by claim 1 is characterized by comprising the following steps of:
step one, continuously metering liquid ammonia, circulating ammonia liquid and ethylene oxide by a mass flow meter, then feeding the liquid ammonia, the circulating ammonia liquid and the ethylene oxide into a high-efficiency pipeline mixer, then feeding the liquid ammonia, the circulating ammonia liquid and the ethylene oxide into a first tubular reactor for reaction, controlling the temperature of materials at 45-60 ℃ after the first-stage reaction is finished, feeding the materials into a first membrane separation assembly, allowing ammonia, water and a small amount of ethanolamine to flow out of a clear liquid end of the first membrane separation assembly, allowing the rest ammonia, water and ethanolamine to flow out of a concentrated liquid end of the membrane separation assembly, and feeding the ammonia, water and ethanolamine to an ammonia still in the next process after passing through a pressure regulating valve and the mass flow meter;
step two, ammonia, water and a small amount of ethanolamine flow out of a clear liquid end of a first membrane separation component D, are pressurized by a first booster pump, enter a second pipeline mixer and then enter a first tubular reactor for reaction, after the second-stage reaction is finished, the temperature of the material is controlled to be 45-60 ℃, and then enter a second membrane separation component, the ammonia, the water and the small amount of ethanolamine flow out of a clear liquid end of the second membrane separation component, the rest ammonia, the water and the ethanolamine flow out of a concentrated liquid end of the membrane separation component, and the ammonia, the water and the ethanolamine flow out of an ammonia still tower in the next process after passing through a pressure regulating valve and a mass flow meter;
step three, allowing ammonia, water and a smaller amount of ethanolamine to flow out of a clear liquid end of a second membrane separation assembly D, pressurizing by a second booster pump, allowing the ammonia, the water and the smaller amount of ethanolamine to enter a third pipeline mixer, allowing the ammonia, the water and the smaller amount of ethanolamine to enter a third tubular reactor for reaction, controlling the temperature of materials to be 45-60 ℃ after the third-stage reaction is finished, allowing the materials to enter a third membrane separation assembly, allowing ammonia liquid to flow out of a clear liquid end of the third membrane separation assembly, pressurizing by a third booster pump, and allowing the ammonia liquid to enter a circulating ammonia liquid pipe to participate in system circulation;
the rest ammonia, water and ethanolamine flow out from the concentrated solution end of the membrane separation component D, pass through a pressure regulating valve and a mass flow meter and then go to an ammonia still in the next procedure.
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Citations (5)
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|---|---|---|---|---|
| CN1863761A (en) * | 2003-10-08 | 2006-11-15 | 巴斯福股份公司 | Method for separating triethanolamin from a mixture obtainable by ammonia and ethylene oxide reaction |
| CN101139295A (en) * | 2007-09-29 | 2008-03-12 | 吴兆立 | Reaction-inhibiting premixing arrangement for ethyloamine production raw materials under high pressure |
| CN101613290A (en) * | 2009-05-12 | 2009-12-30 | 嘉兴金燕化工有限公司 | The improvement of ethanolamine production method |
| CN103772211A (en) * | 2012-10-25 | 2014-05-07 | 中国石油化工股份有限公司 | Method for producing ethanol amine by using liquid ammonia method |
| US20180044308A1 (en) * | 2015-03-05 | 2018-02-15 | Sabic Global Technologies B.V. | Systems and methods related to the production of ethylene oxide, ethylene glycol, and/or ethanolamines |
-
2021
- 2021-12-17 CN CN202111549470.XA patent/CN114276255A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1863761A (en) * | 2003-10-08 | 2006-11-15 | 巴斯福股份公司 | Method for separating triethanolamin from a mixture obtainable by ammonia and ethylene oxide reaction |
| CN101139295A (en) * | 2007-09-29 | 2008-03-12 | 吴兆立 | Reaction-inhibiting premixing arrangement for ethyloamine production raw materials under high pressure |
| CN101613290A (en) * | 2009-05-12 | 2009-12-30 | 嘉兴金燕化工有限公司 | The improvement of ethanolamine production method |
| CN103772211A (en) * | 2012-10-25 | 2014-05-07 | 中国石油化工股份有限公司 | Method for producing ethanol amine by using liquid ammonia method |
| US20180044308A1 (en) * | 2015-03-05 | 2018-02-15 | Sabic Global Technologies B.V. | Systems and methods related to the production of ethylene oxide, ethylene glycol, and/or ethanolamines |
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