CN101260093B - Modified epoxy ethane washing technique for epoxy ethane/ethylene glycol producing device - Google Patents
Modified epoxy ethane washing technique for epoxy ethane/ethylene glycol producing device Download PDFInfo
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- CN101260093B CN101260093B CN2008100505424A CN200810050542A CN101260093B CN 101260093 B CN101260093 B CN 101260093B CN 2008100505424 A CN2008100505424 A CN 2008100505424A CN 200810050542 A CN200810050542 A CN 200810050542A CN 101260093 B CN101260093 B CN 101260093B
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- oxyethane
- ethylene oxide
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Abstract
The invention discloses an improved process for washing ethylene oxide for an ethylene oxide/ethylene glycol production device. Gas is generated through the reaction with ethene, oxygen, carbon dioxide and ethylene oxide in a gas-to-gas heat exchanger and is cooled in a gas feeding cooler of a cooling tower. The cooled gas enters into the cooling tower T1. The process is characterized in that recirculating cooling water is used as the cold medium for cooling the gas cooler E1 of the cooling tower, the gas generated after cooling reaction makes the temperature of the feeding gas generated in the cooling tower T1 drop to between 68 and 72 DEG C. The process has the advantages of effectively reducing the temperature of gas feeding in the cooling tower T1, reducing the loss of ethylene oxide and improving the yields of products; adopting recirculating and cooling water to cool the reaction gas, so as to increase the heat transmittion differnce of the feeding gas cooler of the cooling tower, reduce the heat transmission area, reduce the steam consumption by the stripper reboiler, reduce recirculating cooling water consumption of the recirculating cooling water cooler and increase the heat transmission temperature difference of the recirculating cooling water heat exchanger and further to reduce the heat exchange area and reduce one-time project investment.
Description
Technical field
The oxyethane washing technology that the present invention relates to a kind of ethylene oxide/ethylene glycol production equipment improves technology.
Background technology
The reaction that the outlet of ethylene oxide/ethylene glycol plant reactor contains ethene, oxygen, carbonic acid gas, oxyethane generates gas, about 240 ℃ of temperature, press steam at first producing by the gas reactor water cooler, preheating reaction feed in gas-to-gas heat exchanger then, temperature is reduced to about 85 ℃, cooled gas enters washing tower T1, in washing tower T1 with from the still liquid counter current contact of gas stripping column T2 to absorb oxyethane.The still liquid of washing tower T1 enters gas stripping column to reclaim oxyethane through heating.
For avoiding the gas-to-gas heat exchanger heat exchange efficiency to descend, the circulation gas temperature that causes reactor does not reach the temperature of expection after by gas-to-gas heat exchanger, increased washing tower feed gas water cooler E1, heat-eliminating medium is the still liquid of washing tower T1, to react generation gas wash tower T1 feed gas is cooled to below 72 ℃, self be heated to about 65 ℃, after advancing recirculated water interchanger E3 again and being heated to about 100 ℃ by gas stripping column T2 still liquid, enter into gas stripping column T2 and reclaim oxyethane, its process as shown in Figure 1.
Problem is:
1, recirculated water interchanger E3 thermal load increases, because recirculated water interchanger E3 is limited in one's ability, the temperature that poor recirculated water enters washing tower T1 will not reach the cooling performance of expection, be unfavorable for the absorption of oxyethane;
2, above-mentioned each unit operation conditions each other, fluctuation of service, and device cooling and absorption operating effect are undesirable, are subjected to the influence of other system fluctuation big;
3, the washing water consumption is big, the plant energy consumption height, and the original equipment cost height, one-time investment is big.
For certain gas solute and solvent, Henry'S coefficient changes with temperature.In general, the temperature Henry'S coefficient that raises then increases, and this has embodied the variation tendency that Gas Solubility raises and reduces with temperature.Therefore, reducing the temperature of washing tower T1, promptly reduce the feed gas temperature of washing tower T1 and the temperature of washing liq simultaneously, is the key of dealing with problems.
Oxyethane washing tower T1 in the ethylene oxide/ethylene glycol plant, its temperature height, occur easily that ethylene oxide content exceeds standard in the cat head tail gas, cause ethylene oxide absorption insufficient, the ethylene oxide segment Returning oxidation reactor, deep reaction takes place, and influences the yield of catalyst selectivity and oxyethane.
Summary of the invention
The objective of the invention is to overcome the deficiency of prior art, provide a kind of oxyethane washing technology of ethylene oxide/ethylene glycol production equipment to improve technology.
A kind of oxyethane washing technology of ethylene oxide/ethylene glycol production equipment improves technology, the reaction that contains ethene, oxygen, carbonic acid gas, oxyethane from gas-to-gas heat exchanger generates gas, E1 is cooled at washing tower feed gas water cooler, cooled gas flows into washing tower T1, Ta Nei with from the still liquid counter current contact of gas stripping column T2, to absorb oxyethane, the still liquid of washing tower T1, after recirculated water interchanger E2 and still liquid heat exchange from gas stripping column T2, enter into gas stripping column T2, reclaim oxyethane; The still liquid of gas stripping column T2 is cooled to (area that southern temperature is high can be arrived below 37 ℃) below 34 ℃ through water recirculator E3 again, enters washing tower T1; It is characterized in that:
Adopt the cold medium of recirculated cooling water as washing tower feed gas water cooler E1, the cooling reaction generates gas, and the reaction of washing tower T1 is generated the gas feeding temperature from more than 95 ℃, reduces to 68～72 ℃, and described recirculated cooling water is from plant area's general facilities pipe network.
Advantage of the present invention:
1, reduces the temperature of washing tower T1 gas feed effectively, reduced oxyethane and run off, improved the yield of product;
2, adopt recirculated cooling water cooling reaction to generate gas, increased washing tower feed gas water cooler E1 heat transfer temperature difference, reduced heat transfer area, reduced the material of washing tower feed gas water cooler, thereby reduced facility investment;
3, reduce the washing water consumption of washing tower T1, improved the turndown ratio of washing tower T1; Simultaneously, reduce the steam consumption quantity of gas stripping column reboiler E4 and the consumption of water recirculator E2 recirculated cooling water, thereby reduced the energy consumption of device;
4, reduced the thermal load of water recirculator E2, from the still liquid of the gas stripping column T2 washings as washing tower T1, cooled off fully at this, washing effect obviously improves; Also reduced simultaneously the facility investment of water recirculator E2;
5, increase the heat transfer temperature difference of wash water system recirculated water interchanger E3, thereby can reduce the heat interchanging area of recirculated water interchanger E3, reduced disposable construction investment.
Description of drawings
Fig. 1 is the simplification process flow sheet of existing device.
Fig. 2 simplifies process flow sheet for the present invention.
Washing tower feed gas water cooler E1, water recirculator E2, recirculated water interchanger E3, washing tower T1, gas stripping column T2, gas stripping column reboiler E4 are arranged among the figure
Embodiment
Below in conjunction with the drawings and specific embodiments, the present invention is made detailed description further.
The present invention simplifies technological process such as Fig. 2; The reaction that contains ethene, oxygen, carbonic acid gas, oxyethane from gas-to-gas heat exchanger generates gas, be recycled water quench to 68～72 ℃ through washing tower feed gas water cooler E1, cooled gas flows into washing tower T1, Ta Nei with from the still liquid counter current contact of gas stripping column T2, to absorb oxyethane.The still liquid of washing tower T1 after recirculated water interchanger E3 is heated to about 100 ℃ by the still liquid from gas stripping column, enters into gas stripping column again, to reclaim oxyethane; The still liquid of gas stripping column T2 is cooled to (area that southern temperature is high can be arrived below 37 ℃) below 34 ℃ through water recirculator E2, enters washing tower T1, has obviously improved washing effect.
Adopt the cold medium of recirculated cooling water, will react generation gas wash tower feed gas and be cooled to 68 ℃, washing tower feed gas water cooler E1 tube side material employing stainless steel from 95 ℃ as washing tower feed gas water cooler E1; The shell side material adopts carbon steel; Recirculated water interchanger E3 tube side material adopts stainless steel; The shell side material adopts stainless steel; Water recirculator E2 tube side material adopts stainless steel; The shell side material adopts stainless steel; Washing tower T1 material adopts stainless steel.
Through adjusting, the original equipment cost of device is saved 135.1 ten thousand yuan, the device actual motion shows: ethylene oxide content is reduced to below the 20ppm by 70ppm in the washing tower T1 cat head tail gas, device cooling and absorption operating effect ideal, system operation is stable, the oxyethane rate of recovery is improved significantly, and has reduced the ethylene oxide content in the device discharge of wastewater, effectively reduces raw material consumption and wastewater treatment expense.
Transforming 60,000 tons of/year ethylene oxide device lifes as with 40,000 tons of/year ethylene oxide production plant is example, with the heat-eliminating medium of recirculated cooling water as washing tower feed cooler E1, to react generation gas wash tower T1 charging and be cooled to 72 ℃ from 95 ℃, washing tower feed cooler E1 tube side material adopts stainless steel, the shell side material adopts carbon steel, and heat interchanging area is 230m
2Original equipment cost is saved 45.1 ten thousand yuan than traditional method.
Washing tower T1 charging oxyethane consists of under the actual working conditions of 2.45% (mol), and washing tower T1 cat head ethylene oxide content is 20ppm (mol), washing tower T1 tower base ring oxidative ethane content 1.63% (mol).Traditional method, washing tower T1 charging oxyethane oxyethane consists of under 2.46% (mol) working condition, and washing tower T1 cat head ethylene oxide content is 70ppm (mol), washing tower T1 tower base ring oxidative ethane content 1.62% (mol).
Compare with traditional method, recirculated water is saved 70m
3/ h.The consumption of ton product recirculated water reduces 9m
3/ t oxyethane; The ethene consumption of device reduces about 0.2%, promptly saves 1.7kg ethene/t oxyethane; The original equipment cost of device is saved 45.1 ten thousand yuan, and system obviously descends at the steam that gas bill of lading unit consumes.Device cooling and absorption operating effect ideal.
Adopt washing tower feed cooler E1 process modification technology, the device actual motion shows: reacting ethylene oxide generates good absorbing effect, the efficient height, stable of gas.
With 60,000 tons of/year ethylene oxide devices is example: the washing water consumption has reduced about 5%, and the gas stripping column steam consumption quantity has reduced approximately 8% simultaneously, and it is about 5% that the water recirculator cooling water amount has reduced, and the turndown ratio of washing tower has improved 5%.
Reduced water recirculator E2 thermal load, the poor recirculated water from gas stripping column still liquid is cooled off fully at this, and washing effect obviously improves; Simultaneously, also reduced the facility investment of water recirculator;
It is heat-eliminating medium that washing tower feed gas water cooler E1 adopts rich recirculated water, and rich recirculated water takes this part thermal load to water recirculator E2, adopts recirculated cooling water as heat-eliminating medium, and washing tower T1 overhead gas ethylene oxide content is 20ppm (mol).
The present invention can reduce the water recirculator heat interchanging area, is example with 60,000 tons of/year ethylene oxide devices of a cover: because the minimizing of the thermal load and the washing water yield, heat interchanging area reduces 25%, saves 700,000 yuan of equipment one-time investments.
Increase the heat transfer temperature difference of recirculated water interchanger, and then reduced the facility investment of recirculated water interchanger;
Adopt the present invention, washing tower feed gas water cooler E1 adopts recirculated cooling water as heat-eliminating medium, and described recirculated cooling water also can be the grid that comes from plant area's water cooling tower from plant area's general facilities pipe network; At the bottom of the washing tower rich recirculated water directly with 58 ℃ enter recirculated water interchanger E3 with from the poor recirculated water heat exchange at the bottom of the gas stripping column tower, the temperature difference has improved 7 ℃, the also corresponding minimizing of heat interchanging area for new project, can be saved 200,000 yuan of investments.
Claims (1)
1. the oxyethane washing technology of an ethylene oxide/ethylene glycol production equipment improves technology, the reaction that contains ethene, oxygen, carbonic acid gas, oxyethane from gas-to-gas heat exchanger generates gas, be cooled at washing tower feed gas water cooler (E1), cooled gas flows into washing tower (T1), Ta Nei with from the still liquid counter current contact of gas stripping column (T2), to absorb oxyethane, the still liquid of washing tower (T1), after recirculated water interchanger (E3) and still liquid heat exchange from gas stripping column (T2), enter into gas stripping column (T2), reclaim oxyethane; The still liquid of gas stripping column (T2), be cooled through water recirculator (E2) again, enter washing tower (T1), it is characterized in that: adopt the cold medium of recirculated cooling water as washing tower feed gas water cooler (E1), the cooling reaction generates gas, the reaction generation gas feeding temperature of washing tower (T1) is reduced to 68～72 ℃, and described recirculated cooling water is from plant area's general facilities pipe network.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2008100505424A CN101260093B (en) | 2008-03-21 | 2008-03-21 | Modified epoxy ethane washing technique for epoxy ethane/ethylene glycol producing device |
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| CN2008100505424A CN101260093B (en) | 2008-03-21 | 2008-03-21 | Modified epoxy ethane washing technique for epoxy ethane/ethylene glycol producing device |
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| CN101260093A CN101260093A (en) | 2008-09-10 |
| CN101260093B true CN101260093B (en) | 2010-06-16 |
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Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101875646B (en) * | 2009-04-30 | 2012-01-11 | 中国石油天然气股份有限公司 | Method for cooling ethylene oxide product of ethylene oxide/glycol device |
| CN103275037B (en) * | 2013-05-31 | 2015-08-19 | 嘉兴永明石化有限公司 | The method of a kind of rich ethylene oxide cycle water full gear |
| CN104974113B (en) * | 2014-04-02 | 2017-02-01 | 中国石油化工股份有限公司 | System and method for cooling ethylene oxide absorption water on EO/EG device |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4529417A (en) * | 1981-03-02 | 1985-07-16 | Snamprogetti S.P.A. | Process for the isothermal absorption of ethylene oxide using film absorbers |
| CN86105706A (en) * | 1985-07-03 | 1987-02-25 | 日本触媒化学工业株式会社 | Method for purification ethylene oxide |
-
2008
- 2008-03-21 CN CN2008100505424A patent/CN101260093B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4529417A (en) * | 1981-03-02 | 1985-07-16 | Snamprogetti S.P.A. | Process for the isothermal absorption of ethylene oxide using film absorbers |
| CN86105706A (en) * | 1985-07-03 | 1987-02-25 | 日本触媒化学工业株式会社 | Method for purification ethylene oxide |
Non-Patent Citations (4)
| Title |
|---|
| 卓平等.环氧乙烷吸收塔的改造.石油化工技术经济23 4.2007,23(4),38-41. |
| 卓平等.环氧乙烷吸收塔的改造.石油化工技术经济23 4.2007,23(4),38-41. * |
| 戴忻等.环氧乙烷的吸收与催化水合法制乙二醇.石油化工33 4.2004,33(4),316-319. |
| 戴忻等.环氧乙烷的吸收与催化水合法制乙二醇.石油化工33 4.2004,33(4),316-319. * |
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Effective date of registration: 20170112 Address after: 132022 Jilin, Changyi District, Tong Tong Road, Peng Peng building Patentee after: Jilin Design Institute of Northeast Refining & Chemical Engineering Co., Ltd., CNPC Address before: Changyi District of Jilin city of Jilin Province on the 132022 Road East of Jilin Tan Trade Building Patentee before: Dongbei Branch Co., China Petroleum Group Engineering Designing Co., Ltd. |
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Effective date of registration: 20200925 Address after: 132002 3-6 and 9-13 floors of Block A, Jihua Economic and Trade Center, Tongtan Road, Changyi District, Jilin Province Patentee after: PetroChina Jilin Chemical Engineering Co.,Ltd. Address before: 132022 Jilin, Changyi District, Tong Tong Road, Peng Peng building Patentee before: JILIN DESIGNING INSTITUTE OF CNPC NORTHEAST REFINING & CHEMICAL ENGINEERING Co.,Ltd. |