CN1079820C - Desulfurizing process - Google Patents
Desulfurizing process Download PDFInfo
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- CN1079820C CN1079820C CN98110585A CN98110585A CN1079820C CN 1079820 C CN1079820 C CN 1079820C CN 98110585 A CN98110585 A CN 98110585A CN 98110585 A CN98110585 A CN 98110585A CN 1079820 C CN1079820 C CN 1079820C
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- gas
- carbon monoxide
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- wash tower
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Abstract
The present invention discloses a process for removing hydrogen sulphide and carbon oxysulphide in carbon monoxide. The present invention is characterized in that carbon monoxide containing sulphides with the pressure of 0.1 to 0.35MPa and the temperature of 30 to 40DEGC is added into the bottom of a first alkaline washing tower; simultaneously, 10 to 15% of sodium hydroxide is added from the top of the first alkaline washing tower to come into contact with the carbon monoxide; after hydrogen sulphide in the carbon monoxide is removed, the carbon monoxide is heated to 40 to 60 DEG C in a first steam heater; then, most of carbon oxysulphide in the carbon monoxide is converted to hydrogen sulphide in a primary hydrolysis conversion tower; at the bottom of the lower segment of a second alkaline washing tower, the same processes are operated for three times of desulphurization.
Description
The sulfur removal technology that the present invention relates to, mainly be for produce ditan-4,4 '-hydrogen sulfide, the carbonylsulfide sulfides that contain in the removal of carbon monoxide gas in the vulcabond preorder technology.
The existing ditan-4 of producing, 4 '-the used CO (carbon monoxide converter) gas of vulcabond contains certain sulfide, as hydrogen sulfide, carbonylsulfide etc., because its existence affects the work-ing life of gac catalyst in the phosgene production, increased the corrosion of electrical equipment, instrument, equipment, the most important thing is to have influenced ditan-4,4 '-quality of vulcabond product, distinct issues are that the sulfide in the removal of carbon monoxide just can address the above problem, but find as yet at present.
Purpose of the present invention is intended to improve above-mentioned deficiency, provide a kind of for produce ditan-4,4 '-vulcabond preorder technology removal of carbon monoxide gas in the sulfur removal technology of hydrogen sulfide, carbonylsulfide sulfides.
In order to achieve the above object, the present invention realizes like this, CO (carbon monoxide converter) gas by the manufacturing of carbon monoxide producer, through entering compression section after the dedusting pressure is brought up to 0.1-0.35MPa, temperature is 30-40 ℃, its sulfur removal technology is 0.1-0.35MPa for containing pressure, temperature is the CO (carbon monoxide converter) gas of 30-40 ℃ of sulfide, at first enter the bottom of first soda-wash tower, and the sodium hydroxide that adds 10-15% simultaneously on the first soda-wash tower top contacts with it, behind the hydrogen sulfide in the removal of carbon monoxide gas, enter first steam heater, gas heating is arrived 40-60 ℃, make gas enter the hydrolysis converter one time then, with the most of cos conversion that contains in the gas is hydrogen sulfide, enter the hypomere bottom of second soda-wash tower, the sodium hydroxide that adds 10-15% simultaneously on the hypomere top of second soda-wash tower contacts with it, after removing hydrogen sulfide, gas enters second steam heater again, gas heating is arrived 40-60 ℃, enter secondary hydrolysis converter again, remaining carbonylsulfide is converted into hydrogen sulfide fully, enter the epimere bottom of second soda-wash tower again, and the sodium hydroxide that adds 10-15% simultaneously on the second soda-wash tower epimere top contacts with it, all remove sulfide, the CO (carbon monoxide converter) gas pressure that is come out by cat head is 0.1-0.35MPa, temperature 30-40 ℃, enter ditan-4,4 '-go in the vulcabond production equipment.
Sulfur removal technology principle of work: the CO (carbon monoxide converter) gas that will contain sulfide, remove at first that hydrogen sulfide is laggard goes into the hydrolysis converter, with most of cos conversion is hydrogen sulfide, the CO (carbon monoxide converter) gas that removes behind the hydrogen sulfide enters the hydrolysis converter again, remaining a small amount of carbonylsulfide is converted into hydrogen sulfide fully, the carbon monoxide that removes sulfide send into ditan-4,4 '-the vulcabond production equipment in, whole sulfur removal technology finishes.
Sulfur removal technology of the present invention, contained hydrogen sulfide, the carbonylsulfide of removal of carbon monoxide effectively, can improve the work-ing life of gac catalyst in the phosgene production like this, can reduce the corrosion of electrical equipment, instrument, equipment effectively, more importantly be to have improved ditan-4,4 '-quality of vulcabond, the present invention be produce ditan-4,4 '-vulcabond preorder technology removal of carbon monoxide gas in a kind of more satisfactory sulfur removal technology of sulfide.
In order to understand better and to implement, further specify as follows below with embodiment:
Example 1, CO (carbon monoxide converter) gas by the manufacturing of carbon monoxide producer is brought up to 0.1MPa through entering compression section after the dedusting with pressure, temperature is 30 ℃, be added to the bottom of first soda-wash tower by intake pipeline, and contact with it at the sodium hydroxide NaOH of first soda-wash tower top adding 10% simultaneously, behind the hydrogen sulfide in the removal of carbon monoxide gas, enter first steam heater by intake pipeline, with gas heating to 50 ℃, make gas enter the hydrolysis converter one time then by intake pipeline, with the most of cos conversion that contains in the gas is hydrogen sulfide, enter the hypomere bottom of second soda-wash tower by intake pipeline, and the while contacts with it at the sodium hydroxide of second soda-wash tower hypomere top adding 10%, after removing hydrogen sulfide, pass through intake pipeline, gas enters second steam heater again, with gas heating to 50 ℃, enter secondary hydrolysis converter again by intake pipeline, remaining carbonylsulfide is converted into hydrogen sulfide fully, enter second soda-wash tower epimere bottom again by intake pipeline, and the while contacts with it at the sodium hydroxide of second soda-wash tower epimere top adding 10%, after removing hydrogen sulfide, the CO (carbon monoxide converter) gas pressure that is come out by cat head is 0.1MPa, temperature is 30 ℃, by intake pipeline enter ditan-4,4 '-go in vulcabond (MDI) production equipment.
Example 2, CO (carbon monoxide converter) gas by the manufacturing of carbon monoxide producer is brought up to 0.2MPa through entering compression section after the dedusting with pressure, temperature is 35 ℃, be added to the bottom of first soda-wash tower by intake pipeline, and contact with it at the sodium hydroxide NaOH of first soda-wash tower top adding 12.5% simultaneously, behind the hydrogen sulfide in the removal of carbon monoxide gas, enter first steam heater by intake pipeline, with gas heating to 40 ℃, make gas enter the hydrolysis converter one time then by intake pipeline, with the most of cos conversion that contains in the gas is hydrogen sulfide, enter the hypomere bottom of second soda-wash tower by intake pipeline, and the while contacts with it at the sodium hydroxide of second soda-wash tower hypomere top adding 12.5%, after removing hydrogen sulfide, enter second steam heater again by intake pipeline gas, with gas heating to 40 ℃, enter secondary hydrolysis converter again by intake pipeline, remaining carbonylsulfide is converted into hydrogen sulfide fully, enter second soda-wash tower epimere bottom again by intake pipeline, and the while contacts with it at the sodium hydroxide of second soda-wash tower epimere top adding 12.5%, after removing hydrogen sulfide, the CO (carbon monoxide converter) gas pressure that is come out by cat head is 0.2MPa, temperature is 35 ℃, by intake pipeline enter ditan-4,4 '-go in vulcabond (MDI) production equipment.
Example 3, CO (carbon monoxide converter) gas by the manufacturing of carbon monoxide producer is brought up to 0.35MPa through entering compression section after the dedusting with pressure, temperature is 40 ℃, be added to the bottom of first soda-wash tower by intake pipeline, and contact with it at the sodium hydroxide NaOH of first soda-wash tower top adding 15% simultaneously, behind the hydrogen sulfide in the removal of carbon monoxide gas, enter first steam heater by intake pipeline, with gas heating to 60 ℃, make gas enter the hydrolysis converter one time then by intake pipeline, with the most of cos conversion that contains in the gas is hydrogen sulfide, enter the hypomere bottom of second soda-wash tower by intake pipeline, and the while contacts with it at the sodium hydroxide of second soda-wash tower hypomere top adding 15%, after removing hydrogen sulfide, enter second steam heater again by intake pipeline gas, with gas heating to 60 ℃, enter secondary hydrolysis converter again by intake pipeline, remaining carbonylsulfide is converted into hydrogen sulfide fully, enter second soda-wash tower epimere bottom again by intake pipeline, and the while contacts with it at the sodium hydroxide of second soda-wash tower epimere top adding 15%, after removing hydrogen sulfide, the CO (carbon monoxide converter) gas pressure that is come out by cat head is 0.35MPa, temperature is 40 ℃, by intake pipeline enter ditan-4,4 '-go in vulcabond (MDI) production equipment.
Claims (3)
1, a kind of sulfur removal technology, CO (carbon monoxide converter) gas by the manufacturing of carbon monoxide producer, through entering compression section after the dedusting pressure is brought up to 0.1-0.35MPa, temperature is 30-40 ℃, it is characterized in that containing pressure is 0.1-0.35MPa, temperature is the CO (carbon monoxide converter) gas of 30-40 ℃ of sulfide, at first enter the bottom of first soda-wash tower, and the sodium hydroxide that adds 10-15% simultaneously on the first soda-wash tower top contacts with it, behind the hydrogen sulfide in the removal of carbon monoxide gas, enter first steam heater, gas heating is arrived 40-60 ℃, make gas enter the hydrolysis converter one time then, with the most of cos conversion that contains in the gas is hydrogen sulfide, enter the hypomere bottom of second soda-wash tower, the sodium hydroxide that adds 10-15% simultaneously on the top of the second soda-wash tower hypomere contacts with it, after removing hydrogen sulfide, gas enters second steam heater again, gas heating is arrived 40-60 ℃, enter secondary hydrolysis converter again, remaining carbonylsulfide is converted into hydrogen sulfide fully, enter the epimere bottom of second soda-wash tower again, and the sodium hydroxide that adds 10-15% simultaneously on the second soda-wash tower epimere top contacts with it, all remove sulfide, the CO (carbon monoxide converter) gas pressure that is come out by cat head is 0.1-0.35MPa, temperature 30-40 ℃, enter ditan-4,4 '-go in the vulcabond production equipment.
2, by the described sulfur removal technology of claim 1, the top that it is characterized in that top, the epimere of top, the second soda-wash tower hypomere at first soda-wash tower adds 10% sodium hydroxide and contacts with carbon monoxide.
3, by the described sulfur removal technology of claim 1, it is characterized in that the hydrogen sulfide in the removal of carbon monoxide gas after, enter first, second steam heater by intake pipeline, with gas heating to 50 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN98110585A CN1079820C (en) | 1998-11-23 | 1998-11-23 | Desulfurizing process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN98110585A CN1079820C (en) | 1998-11-23 | 1998-11-23 | Desulfurizing process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1254748A CN1254748A (en) | 2000-05-31 |
| CN1079820C true CN1079820C (en) | 2002-02-27 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN98110585A Expired - Fee Related CN1079820C (en) | 1998-11-23 | 1998-11-23 | Desulfurizing process |
Country Status (1)
| Country | Link |
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| CN (1) | CN1079820C (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE10301434A1 (en) * | 2003-01-16 | 2004-07-29 | Bayer Ag | Process for CO gas desulfurization |
| CN107456852A (en) * | 2017-07-04 | 2017-12-12 | 杨皓 | A kind of technique of carbon dioxide enriched gas conversion desulfurization |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH10194716A (en) * | 1997-01-14 | 1998-07-28 | Teijin Chem Ltd | Purification of carbon monoxide gas |
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1998
- 1998-11-23 CN CN98110585A patent/CN1079820C/en not_active Expired - Fee Related
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH10194716A (en) * | 1997-01-14 | 1998-07-28 | Teijin Chem Ltd | Purification of carbon monoxide gas |
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| Publication number | Publication date |
|---|---|
| CN1254748A (en) | 2000-05-31 |
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| PB01 | Publication | ||
| C53 | Correction of patent for invention or patent application | ||
| COR | Change of bibliographic data |
Free format text: CORRECT: APPLICANT; FROM: YANTAI WANHUA SYNTHETIC LEATHER GROUP CO., LTD TO: YANTAI WANHUA POLYURETHANE CO., LTD. |
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| CP03 | Change of name, title or address |
Address after: No. 2 happy South Road, Shandong, Yantai Applicant after: Yantai Wanhua Polyurethane Co., Ltd. Address before: No. 7 happy South Road, Shandong, Yantai Applicant before: wanhua Synthetic Leather Group Co., Ltd., Yantai |
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