CN102430316A - Method of using methanol exhausted gas as regenerated gas and cold blowing air for temperature swing adsorption - Google Patents
Method of using methanol exhausted gas as regenerated gas and cold blowing air for temperature swing adsorption Download PDFInfo
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- CN102430316A CN102430316A CN2011103648578A CN201110364857A CN102430316A CN 102430316 A CN102430316 A CN 102430316A CN 2011103648578 A CN2011103648578 A CN 2011103648578A CN 201110364857 A CN201110364857 A CN 201110364857A CN 102430316 A CN102430316 A CN 102430316A
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Abstract
The invention discloses a method of using methanol exhausted gas as regenerated gas and cold blowing air for a temperature swing adsorption technical process in a calcium carbide furnace tail gas purifying process. The method mainly comprises the following steps of: (1) recycling hydrogen in methanol exhausted gas by using a pressure swing adsorption hydrogen extraction method in a production technology of producing methanol by purifying calcium carbide furnace tail gas and yellow phosphorus tail gas; (2) leading desorbed tail gas subjected to the pressure swing adsorption hydrogen extraction to serve as cold blowing air in the temperature swing adsorption process; (3) reheating exhaust gas after temperature swing adsorption and cold blowing, and using the heated exhaust gas as regenerated gas for the temperature swing adsorption; and (4) leading regenerated waste gas to enter a waste gas header pipe after the regenerated waste gas comes out of the temperature swing adsorption and is cooled, reaching the standard and discharging the waste gas after burning the waste gas. According to the method, the exhaust gas of the device is used and is made profitable, the problem of air sources of the regenerated gas and the cold blowing air needed for temperature swing adsorption and regeneration is solved, the new pollution generated by using steam for temperature swing adsorption and regeneration in the traditional technology is avoided, and simultaneously the energy consumption of the device and the product cost are reduced.
Description
Technical field
The present invention relates in a kind of production technology,, belong to chemical technology field with methyl alcohol speed the to exit regeneration gas of doing alternating temperature absorption and the method for cold blowing gas with calcium carbide stove exhaust, purifying exhausting gas of yellow phosphorus system methyl alcohol.
Background technology
In the process that calcium carbide stove exhaust, purifying exhausting gas of yellow phosphorus purify with the alternating temperature adsorption method, tail gas alternating temperature adsorption cleaning need pass through normal temperature absorption, thermal regeneration and three steps of cold blowing cooling.The regeneration of the alternating temperature absorption of having gone into operation at present all be with steam as regeneration gas, and steam is condensed into the sewage that contains multiple objectionable impurities after as regeneration gas, need carry out special processing ability qualified discharge.So not only consume steam, and produce the new three wastes.Traditional alternating temperature absorption nitrogen or other waste gas circulation of adopting have increased the energy consumption of device as cold blowing gas like this.
Summary of the invention
The purpose of this invention is to provide a kind of waste gas resource that makes full use of, more environmental protection, cleaner production further reduce the alternating temperature absorption regeneration gas and the cold blowing gas of device operating cost simultaneously.
Above-mentioned purpose of the present invention realizes through following technical scheme: a kind of methyl alcohol speed the to exit regeneration gas of doing alternating temperature absorption and the method for cold blowing gas mainly comprise the steps:
(1) in the production technology of system methyl alcohol, the method for carrying hydrogen with transformation absorption reclaims the hydrogen of methyl alcohol in speeding to exit;
(2) carrying stripping gas behind the hydrogen through step 1 gets in the absorption of tail gas alternating temperature and does cold blowing gas;
(3) heat through the waste gas after step 2 cold blowing, the waste gas after the heating is as the regeneration gas of alternating temperature absorption again;
(4) regeneration off gases goes out alternating temperature absorption cooling back entering waste gas header, removes to burn the back qualified discharge.
As preferably, the system methanol technics described in the step 1 is the production technology that adopts calcium carbide stove exhaust, purifying exhausting gas of yellow phosphorus system methyl alcohol.
Further, heating described in the step 3 is with being heated to 120～400 ℃, preferred 180～250 ℃ through the waste gas behind the cold blowing gas.
The invention has the beneficial effects as follows:
⑴ adopt the methyl alcohol transformation absorption of speeding to exit to carry stripping gas behind the hydrogen as the regeneration gas of alternating temperature absorption, replaced steam as regeneration gas, avoided producing the sewage that contains multiple objectionable impurities, produces the new three wastes, reduced plant energy consumption simultaneously.
(2) adopt the methyl alcohol transformation absorption of speeding to exit to carry stripping gas behind the hydrogen, replaced traditional alternating temperature absorption nitrogen or other waste gas circulation of adopting more, reach and reduce investment and energy saving purposes as cold blowing gas as the cold blowing gas of alternating temperature absorption.
Description of drawings
Fig. 1 is that the embodiment of the invention 1 and 2 is carried stripping gas behind the hydrogen as the method flow sketch map of alternating temperature absorption cold blowing gas and regeneration gas with the methyl alcohol transformation absorption of speeding to exit.
Among Fig. 1, V1 be methyl alcohol speed the venting carry hydrogen system, V2 is calcium carbide stove exhaust or yellow phosphoric tail gas temperature swing adsorption system, E1 is the cold blowing combustion heater, E2 is the regeneration off gases cooler.The 1st, methyl alcohol speeds to exit, and the 2nd, stripping gas (also being cold blowing gas), the 3rd, cold blowing waste gas; The 4th, regeneration gas, the 5th, regeneration off gases, the 6th, discharging gas (be disposed to waste gas header and burn the back qualified discharge); The 7th, hydrogen (hydrogen of from methyl alcohol speeds to exit, purifying can be back to system for methanol synthesis).
The specific embodiment
Below in conjunction with the specific embodiment the present invention is made further detailed description.
But should this be interpreted as that the scope of the above-mentioned theme of the present invention only limits to following embodiment.Do not breaking away under the above-mentioned technological thought situation of the present invention, various replacements or change according to ordinary skill knowledge and customary means are made include within the scope of the invention.
Present embodiment is 100,000 tons of/year methyl alcohol of calcium carbide stove exhaust system, mainly comprises the steps:
(1) in production technology, produces 4300 Nm with 100,000 tons of/year methyl alcohol of calcium carbide stove exhaust system
3The hydrogen of methyl alcohol in speeding to exit is reclaimed in the venting of speeding of/h methyl alcohol, the method for carrying hydrogen with transformation absorption, produces stripping gas 2200 Nm
3/ h;
(2) gassing of separating carried behind the hydrogen of transformation absorption goes to do cold blowing gas in the alternating temperature absorption cold blowing step absorber;
(3) cold blowing waste gas again heater via be warming up to 230 ℃ and get into the heating steps absorbers;
(4) regeneration off gases that goes out absorber goes out to be cooled to 60 ℃ after the alternating temperature absorption and to get into waste gas headers, removes to burn the back qualified discharge.
Present embodiment is 80,000 tons of/year methyl alcohol of yellow phosphoric tail gas system, mainly comprises the steps:
(1) in production technology, produces 3400 Nm with 80,000 tons of/year methyl alcohol of calcium carbide stove exhaust system
3The hydrogen of methyl alcohol in speeding to exit is reclaimed in the venting of speeding of/h methyl alcohol, the method for carrying hydrogen with transformation absorption, produces stripping gas 1800 Nm
3/ h;
(2) gassing of separating carried behind the hydrogen of transformation absorption goes to do cold blowing gas in the alternating temperature absorption cold blowing step absorber;
(3) cold blowing waste gas again heater via be warming up to 380 ℃ and get into the heating steps absorbers;
(4) regeneration off gases that goes out absorber goes out to be cooled to 40 ℃ after the alternating temperature absorption and to get into waste gas headers, removes to burn the back qualified discharge.
Claims (4)
1. a methyl alcohol speed the to exit regeneration gas of doing alternating temperature absorption and the method for cold blowing gas mainly comprises the steps:
(1) in the production technology of system methyl alcohol, the method for carrying hydrogen with transformation absorption reclaims the hydrogen of methyl alcohol in speeding to exit;
(2) carrying stripping gas behind the hydrogen through step 1 gets in the alternating temperature absorption in the calcium carbide tail gas purification process and does cold blowing gas;
(3) heat through the waste gas after step 2 cold blowing, the waste gas after the heating is as the regeneration gas of alternating temperature absorption again;
(4) regeneration off gases goes out alternating temperature absorption cooling back entering waste gas header, removes to burn the back qualified discharge.
2. the method for claim 1, wherein the system methanol technics described in the step 1 is the production technology that adopts calcium carbide stove exhaust, purifying exhausting gas of yellow phosphorus system methyl alcohol.
3. according to claim 1 or claim 2 method, wherein heating described in the step 3 is with being heated to 120～400 ℃, preferred 180～250 ℃ through the waste gas behind the cold blowing gas.
4. like each described method of claim 1-3, wherein the cooling described in the step 4 is that EGT is reduced to 20～100 ℃, preferred 60 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110364857.8A CN102430316B (en) | 2011-11-17 | 2011-11-17 | Method of using methanol exhausted gas as regenerated gas and cold blowing air for temperature swing adsorption |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110364857.8A CN102430316B (en) | 2011-11-17 | 2011-11-17 | Method of using methanol exhausted gas as regenerated gas and cold blowing air for temperature swing adsorption |
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| CN102430316A true CN102430316A (en) | 2012-05-02 |
| CN102430316B CN102430316B (en) | 2014-06-25 |
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| CN201110364857.8A Active CN102430316B (en) | 2011-11-17 | 2011-11-17 | Method of using methanol exhausted gas as regenerated gas and cold blowing air for temperature swing adsorption |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102941075A (en) * | 2012-11-06 | 2013-02-27 | 四川天一科技股份有限公司 | Method for utilizing converter gas adsorption regeneration heat during preparing methyl alcohol by coke-oven gas and converter gas |
| CN103521201A (en) * | 2013-10-09 | 2014-01-22 | 四川天一科技股份有限公司 | Method for regenerating converter gas variable temperature adsorbent for production of methanol from coke oven gas and converter gas |
| CN104474842A (en) * | 2014-11-26 | 2015-04-01 | 四川天一科技股份有限公司 | Temperature swing adsorption method for purifying tail gas of calcium carbide furnace |
| CN109200753A (en) * | 2018-11-13 | 2019-01-15 | 惠州凯美特气体有限公司 | A kind of regeneration technology of improved temperature-change adsorption tower |
Citations (3)
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| CN1680002A (en) * | 2005-02-01 | 2005-10-12 | 四川天一科技股份有限公司 | Pressure varying adsorption of recovering effective components from relaxed methanol gas |
| CN1724369A (en) * | 2005-07-20 | 2006-01-25 | 赵中彦 | Process for producing synthetic ammonia or methanol by acetylene furnace tail gas |
| CN101993339A (en) * | 2010-11-04 | 2011-03-30 | 四川天一科技股份有限公司 | Cold blowing cooling method for converter gas in production of methyl alcohol by using coke-oven gas and converter gas |
-
2011
- 2011-11-17 CN CN201110364857.8A patent/CN102430316B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1680002A (en) * | 2005-02-01 | 2005-10-12 | 四川天一科技股份有限公司 | Pressure varying adsorption of recovering effective components from relaxed methanol gas |
| CN1724369A (en) * | 2005-07-20 | 2006-01-25 | 赵中彦 | Process for producing synthetic ammonia or methanol by acetylene furnace tail gas |
| CN101993339A (en) * | 2010-11-04 | 2011-03-30 | 四川天一科技股份有限公司 | Cold blowing cooling method for converter gas in production of methyl alcohol by using coke-oven gas and converter gas |
Non-Patent Citations (1)
| Title |
|---|
| 曹凯等: "不同原料制甲醇的能值分析与比较", 《化工进展》 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102941075A (en) * | 2012-11-06 | 2013-02-27 | 四川天一科技股份有限公司 | Method for utilizing converter gas adsorption regeneration heat during preparing methyl alcohol by coke-oven gas and converter gas |
| CN102941075B (en) * | 2012-11-06 | 2014-07-09 | 四川天一科技股份有限公司 | Method for utilizing converter gas adsorption regeneration heat during preparing methyl alcohol by coke-oven gas and converter gas |
| CN103521201A (en) * | 2013-10-09 | 2014-01-22 | 四川天一科技股份有限公司 | Method for regenerating converter gas variable temperature adsorbent for production of methanol from coke oven gas and converter gas |
| CN104474842A (en) * | 2014-11-26 | 2015-04-01 | 四川天一科技股份有限公司 | Temperature swing adsorption method for purifying tail gas of calcium carbide furnace |
| CN109200753A (en) * | 2018-11-13 | 2019-01-15 | 惠州凯美特气体有限公司 | A kind of regeneration technology of improved temperature-change adsorption tower |
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| Publication number | Publication date |
|---|---|
| CN102430316B (en) | 2014-06-25 |
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Address after: 610225 Technology Innovation Service Center of Chengdu High-tech Zone, Chengdu, Sichuan Province, No. 5 Gaopeng Avenue, Chengdu High-tech Zone Patentee after: Haohua Chemical Technology Group Co., Ltd. Address before: 610225 No. 5 Gaopeng Avenue, Chengdu High-tech Development Zone, Sichuan Province Patentee before: Tianyi Science and Technology Co., Ltd., Sichuan Prov |
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Effective date of registration: 20200422 Address after: No. 5 high tech Zone Gaopeng road in Chengdu city of Sichuan Province in 610041 Patentee after: SOUTHWEST RESEARCH & DESIGN INSTITUTE OF CHEMICAL INDUSTRY Address before: 610225 Technology Innovation Service Center of Chengdu High-tech Zone, Chengdu, Sichuan Province, No. 5 Gaopeng Avenue, Chengdu High-tech Zone Patentee before: Haohua Chemical Technology Group Co., Ltd. |
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