CN102745646A - Method for replenishing sulfureted hydrogen during CO transformation production process - Google Patents
Method for replenishing sulfureted hydrogen during CO transformation production process Download PDFInfo
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- CN102745646A CN102745646A CN2012101814686A CN201210181468A CN102745646A CN 102745646 A CN102745646 A CN 102745646A CN 2012101814686 A CN2012101814686 A CN 2012101814686A CN 201210181468 A CN201210181468 A CN 201210181468A CN 102745646 A CN102745646 A CN 102745646A
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Abstract
The invention relates to a method for replenishing sulfureted hydrogen during a CO transformation production process. According to the invention, a concentrated sulfuric acid storage tank, a concentrated sulfuric acid metering pump, a dilute sulphuric acid preparation tank, a sodium sulfide preparation tank, a sodium sulfide storage tank, a sodium sulfide metering pump, a sulfureted hydrogen generator, a conversion gas pipeline and a feed gas header pipe are successively connected. A sulfureted hydrogen generation system is established to replenish sulfureted hydrogen for feed gas, so that the content of the sulfureted hydrogen contained in the feed gas meets the requirement of the technology of conversion and purification of carbide furnace gas. Therefore, an overall low temperature shift devulcanization phenomenon can be avoided and thus the transformation efficiency of the carbide furnace gas and the quality of the transformed gas can be improved. Moreover, the equipment employed in the method is less; the process is simple and reasonable; and the method is easy to be implemented. The provided method can be widely applied to the overall low temperature shift Co transformation process and is especially suitable for the sulfureted hydrogen replenishing process of a carbide furnace gas desulphurization system.
Description
Technical field:
The present invention relates to a kind of CO of being used for conversion and produce the method for mending hydrogen sulfide, particularly be applicable in the additional hydrogen sulfide operation of calcium carbide furnace gas desulphurization system.
Background technology:
The virgin gas that Xingjiang Tianye Co.'s BDO-EG project is used is calcium carbide furnace gas, and the calcium carbide furnace gas flow is 30000m
3/ h, project adopts complete low CO conversion and desulfurization and decarburization technology, the about 2mg/m of total sulfur content in the calcium carbide furnace gas of becoming
3, requiring the virgin gas total sulfur content when adopting full low temperature shift process is 150mg/m
3, the total sulfur content deficiency can cause the complete low reversal of cure that becomes, and the hydrogen sulfide amount in decarbonization, desulfuration system regeneration gas accounts for 95% of transformation system total sulfur content, and the hydrogen sulfide loss amount is about 5%, returns that the virgin gas total sulfur content is 144.5mg/m behind the conversion process
3, therefore need to replenish hydrogen sulfide and be about 5.5mg/m
3, be 30000m by the calcium carbide furnace gas flow
3/ h calculates, and per hour need replenish hydrogen sulfide is 165g.
Summary of the invention:
The invention solves in calcium carbide furnace gas conversion, the purification process, because of hydrogen sulfide loss in the decarbonization, desulfuration system causes the virgin gas total sulfur content less than 150mg/m
3Problem, adopt the hydrogen sulfide generation systems in virgin gas, to replenish hydrogen sulfide, make hydrogen sulfide content in the virgin gas satisfy the requirement of calcium carbide furnace gas conversion and purification process, the quality of the conversion of raising calcium carbide furnace gas, purification efficiency and conversion gas.
The technical scheme that the present invention adopts is: the method for mending hydrogen sulfide is produced in a kind of CO of being used for conversion of the present invention, comprises the vitriol oil storage tank, vitriol oil volume pump, dilute sulphuric acid Preparation tank, sodium sulphite configured slot, sodium sulphite storage tank, sodium sulphite volume pump, hydrogen sulfide generator, conversion feed channel, the virgin gas house steward that link to each other successively; The vitriol oil in the vitriol oil storage tank gets into the dilute sulphuric acid Preparation tank through the metering back, and to be mixed with concentration be 10% dilute sulphuric acid, and dilute sulphuric acid is injected hydrogen sulfide generator according to the amount of 3.0～8.0kg per hour; Then the 50kg solid sodium sulfide of accurate weighing is put into the sodium sulphite Preparation tank; Injection 285kg temperature is 35 ℃～45 ℃ a warm water; Stir, can be mixed with concentration and be 15% sodium sulfide solution, after sodium sulfide solution prepares on demand amount inject the sodium sulphite storage tank; Through the sodium sulphite volume pump solution is injected hydrogen sulfide generator, the volume pump flow control is 1.0～10.0L/h; Last dilute sulphuric acid and sodium sulfide solution fully react in hydrogen sulfide generator and generate hydrogen sulfide, and the hydrogen sulfide of generation is introduced the virgin gas house steward with conversion gas.
Described a kind of method that benefit hydrogen sulfide is produced in the CO conversion that is used for according to full low temperature shift process requirement, need be 4.0～10.0mg/m to the amount of the additional hydrogen sulfide of virgin gas house steward
3
Described a kind of method that benefit hydrogen sulfide is produced in the CO conversion that is used for, conversion gas residence time in hydrogen sulfide generator is about 1.5min, and needing conversion gas total flux is 100m
3/ h.
Described a kind of method that benefit hydrogen sulfide is produced in the CO conversion that is used for, the hydrogen sulfide generator cubic capacity is 6m
3, the about 5.0m of the shared volume of reaction soln wherein
3, gas-phase space is about 1.0m
3, be 750h a duration of service.
Described a kind of method that benefit hydrogen sulfide is produced in the CO conversion that is used for, disposable implantation concentration is 10% dilute sulphuric acid 3600kg in hydrogen sulfide generator, the dilute sulphuric acid consumption per hour is 3.0～8.0kg.
Described a kind of method that benefit hydrogen sulfide is produced in the CO conversion that is used for, the sodium sulfide solution volume pump per hour selects for use 0～10L adjustable, and the volume pump motor adopts speed control by frequency variation.
The present invention is through setting up the hydrogen sulfide generation systems; In virgin gas, replenish hydrogen sulfide; Make hydrogen sulfide content in the virgin gas satisfy the requirement of calcium carbide furnace gas conversion and purification process, avoided the complete low reversal of cure that becomes, improve the quality of calcium carbide furnace gas conversion efficiency and conversion gas.Present device is few, technology advantages of simple, easy to implement, can be widely used in particularly being applicable in the additional hydrogen sulfide operation of calcium carbide furnace gas desulphurization system in the complete low CO of the change shift conversion step.
Description of drawings:
Fig. 1 is the embodiments of the invention process flow sheet;
Among Fig. 1: 1 is that vitriol oil storage tank, 2 is that vitriol oil volume pump, 3 is that dilute sulphuric acid Preparation tank, 4 is that sodium sulphite configured slot, 5 is that sodium sulphite storage tank, 6 is that sodium sulphite volume pump, 7 is that hydrogen sulfide generator, 8 is that conversion feed channel, 9 is the virgin gas house steward;
Specific embodiments:
With reference to accompanying drawing 1, present embodiment comprises vitriol oil storage tank 1, vitriol oil volume pump 2, dilute sulphuric acid Preparation tank 3, sodium sulphite configured slot 4, sodium sulphite storage tank 5, sodium sulphite volume pump 6, hydrogen sulfide generator 7, conversion feed channel 8, the virgin gas house steward 9 who links to each other successively; The vitriol oil in the vitriol oil storage tank gets into the dilute sulphuric acid Preparation tank through the metering back, and to be mixed with concentration be 10% dilute sulphuric acid, and dilute sulphuric acid is injected hydrogen sulfide generator according to the amount of 3.0～8.0kg per hour; Then the 50kg solid sodium sulfide of accurate weighing is put into the sodium sulphite Preparation tank; Injection 285kg temperature is 35 ℃～45 ℃ a warm water; Stir, can be mixed with concentration and be 15% sodium sulfide solution, after sodium sulfide solution prepares on demand amount inject the sodium sulphite storage tank; Through the sodium sulphite volume pump solution is injected hydrogen sulfide generator, the volume pump flow control is 1.0～10.0L/h; Last dilute sulphuric acid and sodium sulfide solution fully react in hydrogen sulfide generator and generate hydrogen sulfide, and the hydrogen sulfide of generation is introduced the virgin gas house steward with conversion gas.
Another embodiment difference is that dilute sulphuric acid concentration is 15%, and sodium sulfide solution concentration is 20%;
Another embodiment difference is that dilute sulphuric acid concentration is 25%, and sodium sulfide solution concentration is 30%;
Another embodiment difference is that dilute sulphuric acid concentration is 40%, and sodium sulfide solution concentration is 45%.
Claims (8)
1. one kind is used for the method that benefit hydrogen sulfide is produced in the CO conversion, comprises the vitriol oil storage tank, vitriol oil volume pump, dilute sulphuric acid Preparation tank, sodium sulphite configured slot, sodium sulphite storage tank, sodium sulphite volume pump, hydrogen sulfide generator, conversion feed channel, the virgin gas house steward that link to each other successively; It is characterized in that: vitriol oil storage tank and dilute sulphuric acid Preparation tank are used to be mixed with certain density dilute sulphuric acid; Sodium sulphite Preparation tank and sodium sulphite storage tank are used to be mixed with certain density sodium sulfide solution; The sodium sulphite volume pump is used for accurate measurement sodium sulfide solution flow; Hydrogen sulfide generator is used for dilute sulphuric acid and sodium sulfide solution fully reacts the generation hydrogen sulfide, and the hydrogen sulfide of generation is introduced the virgin gas house steward with conversion gas.
2. according to claims 1 described a kind of method that benefit hydrogen sulfide is produced in the CO conversion that is used for, it is characterized in that: the amount of replenishing hydrogen sulfide to the virgin gas house steward is 4.0～10.0mg/m
3
3. according to claims 1 described a kind of method that benefit hydrogen sulfide is produced in the CO conversion that is used for, it is characterized in that: conversion gas total flux is 50～200m
3/ h.
4. according to claims 1 described a kind of method that benefit hydrogen sulfide is produced in the CO conversion that is used for, it is characterized in that: the concentration of dilute sulphuric acid is 10%～40%.
5. according to claims 4 described a kind of methods that benefit hydrogen sulfide is produced in the CO conversion that are used for, it is characterized in that: the dilute sulphuric acid consumption per hour is 3.0～8.0kg.
6. according to claims 1 described a kind of method that benefit hydrogen sulfide is produced in the CO conversion that is used for, it is characterized in that: sodium sulfide solution concentration is 15%～45%.
7. according to claims 6 described a kind of methods that benefit hydrogen sulfide is produced in the CO conversion that are used for, it is characterized in that: sodium sulphite volume pump working control flow is 1.0～10.0L/h.
8. according to the described a kind of method that benefit hydrogen sulfide is produced in the CO conversion that is used for of claims 1-7, it is characterized in that: the virgin gas total sulfur content is 145～200mg/m behind the additional hydrogen sulfide
3
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| CN2012101814686A CN102745646A (en) | 2012-06-05 | 2012-06-05 | Method for replenishing sulfureted hydrogen during CO transformation production process |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105776137A (en) * | 2016-02-17 | 2016-07-20 | 新疆天智辰业化工有限公司 | Method for supplementing sulfur to CO shift catalyst by replacing carbon disulfide with liquid sulfur |
| CN114440136A (en) * | 2022-03-07 | 2022-05-06 | 上海照潇环保科技有限公司 | Centralized liquid supply system |
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| CN1051896A (en) * | 1989-11-16 | 1991-06-05 | 新金县化肥厂 | Sulphur resisting and low temp conversing processes and reactor |
| CN1429763A (en) * | 2001-12-30 | 2003-07-16 | 中国石化集团齐鲁石油化工公司 | CO sulfur resistant transformation catalyst and its preparation method |
| CN101337682A (en) * | 2008-06-20 | 2009-01-07 | 天津市大港亿中化工厂 | Ammonium sulfide solution and processing process thereof |
| CN101434379A (en) * | 2008-12-15 | 2009-05-20 | 四川天一科技股份有限公司 | Coke-oven gas transform processing method |
| EP2248575A1 (en) * | 2009-04-30 | 2010-11-10 | Mitsubishi Heavy Industries | Method and system for recovering high-purity CO2 from gasification gas |
| CN101973521A (en) * | 2010-09-21 | 2011-02-16 | 江阴市尚疯新能源技术开发有限公司 | Method for forming oxygen and hydrogen by using steam and carbon monoxide through regenerating reduction and circular gasification |
-
2012
- 2012-06-05 CN CN2012101814686A patent/CN102745646A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1051896A (en) * | 1989-11-16 | 1991-06-05 | 新金县化肥厂 | Sulphur resisting and low temp conversing processes and reactor |
| CN1429763A (en) * | 2001-12-30 | 2003-07-16 | 中国石化集团齐鲁石油化工公司 | CO sulfur resistant transformation catalyst and its preparation method |
| CN101337682A (en) * | 2008-06-20 | 2009-01-07 | 天津市大港亿中化工厂 | Ammonium sulfide solution and processing process thereof |
| CN101434379A (en) * | 2008-12-15 | 2009-05-20 | 四川天一科技股份有限公司 | Coke-oven gas transform processing method |
| EP2248575A1 (en) * | 2009-04-30 | 2010-11-10 | Mitsubishi Heavy Industries | Method and system for recovering high-purity CO2 from gasification gas |
| CN101973521A (en) * | 2010-09-21 | 2011-02-16 | 江阴市尚疯新能源技术开发有限公司 | Method for forming oxygen and hydrogen by using steam and carbon monoxide through regenerating reduction and circular gasification |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105776137A (en) * | 2016-02-17 | 2016-07-20 | 新疆天智辰业化工有限公司 | Method for supplementing sulfur to CO shift catalyst by replacing carbon disulfide with liquid sulfur |
| CN114440136A (en) * | 2022-03-07 | 2022-05-06 | 上海照潇环保科技有限公司 | Centralized liquid supply system |
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