CN104118847A - Synthesizer starting method completing 2.4 MPa shift by utilization of low-pressure steam - Google Patents
Synthesizer starting method completing 2.4 MPa shift by utilization of low-pressure steam Download PDFInfo
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- CN104118847A CN104118847A CN201410312568.7A CN201410312568A CN104118847A CN 104118847 A CN104118847 A CN 104118847A CN 201410312568 A CN201410312568 A CN 201410312568A CN 104118847 A CN104118847 A CN 104118847A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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Abstract
The invention discloses a synthesizer starting method completing 2.4 MPa shift by utilization of low-pressure steam, and relates to the technical field of chemical engineering. Gas making, system inert gas displacement and starting are achieved by utilization of steam having a pressure of 1.0 MPa of a neighbor company. Heating sulfuration of a shift catalytic agent is performed so as to allow the catalytic agent to have production capability. Then the pressure of a shift system is controlled to be 0.8 MPa, and prepared qualified shift gas is added by utilization of the steam having a pressure of 1.0 MPa. CO2 removing is performed under a pressure of 0.8 MPa to prepare qualified purified gas so as to meet requirements of heating reduction of catalytic agents in alcohol alkylation systems.
Description
Technical field
The present invention relates to chemical technology field, be specifically related to a kind of synthesizer starting method that utilizes low-pressure steam to complete 2.4MPa conversion.
Background technology
240,000 tons of synthetic ammonia installations of our company are designed to: adopt fixed bed gas processed, and the de-technique of the conversion of 2.4MPa and change, pressure swing adsorption decarbonization, height compressor separates, 20.0MPa high pressure alcohol alkanisation and ammonia synthesis.What adopt due to conversion is the full low temperature shift process of 2.4MPa, and this will ask the transformation system vapor pressure grade used will be higher than 2.5MPa.But the design of boiler, erection schedule could not be synchronous, at least one month can put into operation.Synthetic ammonia is eager again to drive to produce, and for the steam supply during ensureing to drive, has laid the vapour line of a long 3.0MPa of 2.5 km from contiguous company, and peak flow is designed to 60T/ hour.But do not have ditch to have friendly relations when installing at that time, I do not understand the steam system flow process of contiguous company by company's installation personnel, cause cannot supplying with the steam of 3.0MPa after pipeline laying finishes, can only supply the superheated vapour of 1.0MPa, this has just determined that synthetic ammonia does not possess initial start-up condition substantially.
Summary of the invention
Technical problem to be solved by this invention is to provide a kind of synthesizer starting method that utilizes low-pressure steam to complete 2.4MPa conversion.
Technical problem to be solved by this invention realizes by the following technical solutions:
Utilize low-pressure steam to complete a synthesizer starting method for 2.4MPa conversion, concrete grammar is as follows:
The superheated vapour of the 1.0MPa of the contiguous company of utilization supply, as vapour source, in the heating reduction process of ammonia synthesis, due to furnace power deficiency, improves as far as possible and converts pressure to 0.9MPa left and right, improves as far as possible system tolerance;
Next closes useless pot vapour outlet valve, allow useless pot pressure slowly suppress height, reach after 3.0MPa until useless pot pressure, close rapidly the steam valve of 1.0MPa, open useless pot outlet valve and send steam toward conversion, the vapor pressure that now useless pot is sent can reach 2.2MPa left and right to conversion, at this moment the rapid dosage of compressor is to converting pressure 1.2MPa, after dosage, synthetic fresh tolerance increases, reaction heat increases, useless pot goes out vapor pressure and can be stabilized in the steam of 1.4-1.5MPa, now slowly improve transformation system pressure on one side to vapor pressure, improve as far as possible tolerance, when improving tolerance, synthesising reacting heat is also increasing, useless pot goes out vapor pressure also slowly to be increased,
Vapor pressure is in slowly improving like this, and transformation system pressure increases thereupon, finally makes and so forth to convert pressure and reaches 2.0MPa left and right, and synthesis system tolerance also can meet initial start-up needs, has completed smoothly the startup procedure of whole synthetic ammonia installation.
The invention has the beneficial effects as follows:
1, the steam that is 1.0MPa with contiguous company pressure, has completed gas making, the lazy displacement of system of system, driving work.
2, complete conversion catalyst intensification sulfuration work, make it possess throughput, then transformation system pressure-controlling at 0.8MPa, add and produce qualified conversion gas with 1.0MPa steam.
3, under 0.8MPa pressure, complete CO2 and remove work, make qualified purified gas, to meet alcohol alkanisation system catalyst heating reduction needs.
4, complete alcohol alkanisation, revivification of catalyst work.
Embodiment
For technique means, creation characteristic that the present invention is realized, reach object and effect is easy to understand, below in conjunction with specific embodiment, further set forth the present invention.
Embodiment 1
Utilize low-pressure steam to complete the synthesizer starting method that 2.4MPa converts, detailed process:
1, the steam that is 1.0MPa with contiguous company pressure, has completed gas making, the lazy displacement of system of system, driving work.
2, complete the intensification sulfuration work of conversion catalyst, make it possess throughput.Then transformation system pressure-controlling at 0.8MPa, add and produce qualified conversion gas with 1.0MPa steam.
3, under 0.8MPa pressure, complete CO2 and remove work, make qualified purified gas, to meet alcohol alkanisation system catalyst heating reduction needs.
4, complete alcohol alkanisation, revivification of catalyst work.
5, in the heating reduction process of ammonia synthesis, due to furnace power deficiency, improve conversion pressure to 0.9MPa left and right as far as possible, improve as far as possible system tolerance.
Next closes useless pot vapour outlet valve, allow useless pot pressure slowly suppress height, reach after 3.0MPa until useless pot pressure, close rapidly China and mould the steam valve of 1.0MPa, open useless pot outlet valve and send steam toward conversion, the vapor pressure that now useless pot is sent can reach 2.2MPa left and right to conversion, at this moment the rapid dosage of compressor is to converting pressure 1.2MPa, after dosage, synthetic fresh tolerance increases, reaction heat increases, useless pot goes out vapor pressure and can be stabilized in the steam of 1.4-1.5MPa, now slowly improve transformation system pressure on one side to vapor pressure, improve as far as possible tolerance, when improving tolerance, synthesising reacting heat is also increasing, useless pot goes out vapor pressure also slowly to be increased.
Vapor pressure is in slowly improving like this, transformation system pressure increases thereupon, finally make and so forth to convert pressure and reach 2.0MPa left and right, synthesis system tolerance also can meet initial start-up needs, has completed smoothly the startup procedure of whole synthetic ammonia installation.
Because boiler just built up and comes into operation at after this 1 month, this time the driving time has been shifted to an earlier date 1 month in fact, and economic benefit, the social benefit of increase cannot be estimated.
The success of this low pressure driving method, is first the innovation in thinking, i.e. the conversion of 2.4MPa and pressure swing adsorption purge technique complete driving work under the pressure of 0.8MPa; Next is technical innovation, has used many unconventional technology in driving link, has also obtained every expert's support energetically; Especially all cadres and masses of company and industry specialists day and night, the wisdom crystallization of making nothing of hardships.
More than show and described ultimate principle of the present invention and principal character and advantage of the present invention.The technician of the industry should understand; the present invention is not restricted to the described embodiments; that in above-described embodiment and specification sheets, describes just illustrates principle of the present invention; without departing from the spirit and scope of the present invention; the present invention also has various changes and modifications, and these changes and improvements all fall in the claimed scope of the invention.The claimed scope of the present invention is defined by appending claims and equivalent thereof.
Claims (1)
1. utilize low-pressure steam to complete a synthesizer starting method for 2.4MPa conversion, it is characterized in that: concrete grammar is as follows:
The superheated vapour of the 1.0MPa of the contiguous company of utilization supply, as vapour source, in the heating reduction process of ammonia synthesis, due to furnace power deficiency, improves as far as possible and converts pressure to 0.9MPa left and right, improves as far as possible system tolerance;
Next closes useless pot vapour outlet valve, allow useless pot pressure slowly suppress height, reach after 3.0MPa until useless pot pressure, close rapidly the steam valve of 1.0MPa, open useless pot outlet valve and send steam toward conversion, the vapor pressure that now useless pot is sent can reach 2.2MPa left and right to conversion, at this moment the rapid dosage of compressor is to converting pressure 1.2MPa, after dosage, synthetic fresh tolerance increases, reaction heat increases, useless pot goes out vapor pressure and can be stabilized in the steam of 1.4-1.5MPa, now slowly improve transformation system pressure on one side to vapor pressure, improve as far as possible tolerance, when improving tolerance, synthesising reacting heat is also increasing, useless pot goes out vapor pressure also slowly to be increased,
Vapor pressure is in slowly improving like this, and transformation system pressure increases thereupon, finally makes and so forth to convert pressure and reaches 2.0MPa left and right, and synthesis system tolerance also can meet initial start-up needs, has completed smoothly the startup procedure of whole synthetic ammonia installation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410312568.7A CN104118847B (en) | 2014-07-02 | 2014-07-02 | Low-pressure steam is utilized to complete the synthesizer starting method of 2.4MPa conversion |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410312568.7A CN104118847B (en) | 2014-07-02 | 2014-07-02 | Low-pressure steam is utilized to complete the synthesizer starting method of 2.4MPa conversion |
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| Publication Number | Publication Date |
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| CN104118847A true CN104118847A (en) | 2014-10-29 |
| CN104118847B CN104118847B (en) | 2016-01-06 |
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| CN201410312568.7A Active CN104118847B (en) | 2014-07-02 | 2014-07-02 | Low-pressure steam is utilized to complete the synthesizer starting method of 2.4MPa conversion |
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Citations (4)
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|---|---|---|---|---|
| CN102618332A (en) * | 2011-12-23 | 2012-08-01 | 航天长征化学工程股份有限公司 | Starting/stopping control method and system for powdered coal pressure gasification device |
| CN102807233A (en) * | 2012-08-30 | 2012-12-05 | 安徽淮化股份有限公司 | Method for shortening low-temperature methanol wash and liquid nitrogen wash starting time during production of synthesis ammonia and device system for implementing method |
| CN102994162A (en) * | 2012-12-10 | 2013-03-27 | 中国五环工程有限公司 | Circulating fluidized bed gasifier system and starting method thereof |
| CN103570494A (en) * | 2013-11-21 | 2014-02-12 | 七台河宝泰隆甲醇有限公司 | Method for starting methanol synthesis tower through reverse steam guiding |
-
2014
- 2014-07-02 CN CN201410312568.7A patent/CN104118847B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102618332A (en) * | 2011-12-23 | 2012-08-01 | 航天长征化学工程股份有限公司 | Starting/stopping control method and system for powdered coal pressure gasification device |
| CN102807233A (en) * | 2012-08-30 | 2012-12-05 | 安徽淮化股份有限公司 | Method for shortening low-temperature methanol wash and liquid nitrogen wash starting time during production of synthesis ammonia and device system for implementing method |
| CN102994162A (en) * | 2012-12-10 | 2013-03-27 | 中国五环工程有限公司 | Circulating fluidized bed gasifier system and starting method thereof |
| CN103570494A (en) * | 2013-11-21 | 2014-02-12 | 七台河宝泰隆甲醇有限公司 | Method for starting methanol synthesis tower through reverse steam guiding |
Non-Patent Citations (4)
| Title |
|---|
| 刘鸿元: "1850t/dKAAP合成氨装置技术特点及开车运行情况", 《川化》, no. 4, 31 December 1999 (1999-12-31), pages 10 - 14 * |
| 孙翔: "合成氨装置开车过程中问题分析及对策", 《大氮肥》, vol. 34, 30 September 2011 (2011-09-30), pages 43 - 48 * |
| 袁国山: "Ф1200mm氨合成装置运行总结", 《小氮肥》, vol. 38, no. 9, 30 September 2010 (2010-09-30), pages 5 - 8 * |
| 黄夏威: "合成氨低压联醇系统开车技术总结", 《化肥工业》, no. 6, 30 June 2012 (2012-06-30), pages 52 - 55 * |
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| CN104118847B (en) | 2016-01-06 |
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