CN204958384U - Mix coal gas clean system - Google Patents
Mix coal gas clean system Download PDFInfo
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- CN204958384U CN204958384U CN201520675943.4U CN201520675943U CN204958384U CN 204958384 U CN204958384 U CN 204958384U CN 201520675943 U CN201520675943 U CN 201520675943U CN 204958384 U CN204958384 U CN 204958384U
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Abstract
The utility model discloses a mix coal gas clean system, wash device, pressure swing adsorption unit, methane steam reforming CO converting means including transform cooling device, two at least prewashing devices, low temperature methanol washing desulfurizing tower, low temperature methanol washing decarbonization tower, liquid nitrogen, prewashing device and transform cooling device intercommunication, air inlet and each prewashing device intercommunication of desulfurizing tower, the gas outlet of desulfurizing tower communicates with pressure swing adsorption unit and decarbonization tower respectively, the intercommunication of device is washed respectively to methane steam reforming CO converting means's air inlet with pressure swing adsorption unit and liquid nitrogen, the all mistakes of this department increase the handling capacity of mixed coal gas of prewashing stage to divide two the tunnel to carry out purification treatment behind desulfurization process the coal gas after the prewashing, through the quantity of adjustment prewashing device, the gas conditioning volume that the aperture just can improve mix coal gas clean system, effective ability of mixing the gas purifying and being H2 that improves need not to change follow -up equipment, has avoided parallelly connected second to overlap the huge investment that the device was washed to low temperature methanol washing and liquid nitrogen.
Description
Technical field
The utility model belongs to coal gas comprehensive application technology field, particularly relates to a kind of purification system mixed gas being prepared pure hydrogen through desulfurization, decarburization.
Background technology
Pressurization alternating temperature continuous coking and gasification mixed gas are a kind of special coal gas, and the coal gas composition of the coke(oven)gas produced with coking of coal, improving quality of coal by pyrolysis by-product is similar.The feature of this mixed gas mainly containing 8 ~ 12% methane fraction, should desulfurization and decarburization when processing treatment hydrogen making, must methane conversion/conversion be carried out simultaneously.
Along with mixed gas is to the infiltration and development in organic chemical industry field, high to the purity requirement of hydrogen, demand is large, but the problems such as existing mixed gas hydrogen technology ubiquity processing treatment coal is narrow-minded, if as increased hydrogen output, a set of low-temperature rectisol in parallel and liquid nitrogen washing device again, investment cost is expensive, coal gas is improved to the cost of hydrogen gas, does not have feasibility.Therefore, for meeting the needs of synthetic ammonia (methyl alcohol) production and organic chemical industry's hydrogenation, require to be optimized configuration to purification process, the purification process that ammonia (alcohol) hydrogen combines needs exploitation further.
Summary of the invention
In order to overcome problems of the prior art, the utility model discloses a kind of novel mixed gas purification system, by coal gas after the conversion of sulfur-resisting transformation refrigerating unit, after abundant prewashing, carrying out desulfurization, decarburization obtains high-purity hydrogen.
The utility model is achieved by the following technical solution:
A kind of mixed gas purification system, comprises conversion refrigerating unit, prewashing device, thionizer, decarbonizing tower, liquid nitrogen washing device, pressure-swing absorption apparatus and methane steam reforming/CO changing device, wherein:
Conversion refrigerating unit, for carrying out conversion cooling process by the mixed gas in device;
At least two prewashing devices, described prewashing device is communicated with conversion refrigerating unit, carries out pre-treatment for being assigned in each prewashing device by the part mixed gas through the process of conversion refrigerating unit;
Thionizer, the inlet mouth of described thionizer is communicated with each prewashing device, the air outlet of described thionizer is communicated with decarbonizing tower with pressure-swing absorption apparatus respectively, the air outlet of described decarbonizing tower is communicated with liquid nitrogen washing device, for carrying out desulfurization process by the gas collection in each prewashing device to thionizer, gas after desulfurization is divided into two-way to carry out purifying treatment and obtain hydrogen; Certainly, pipeline connection can be passed through between described thionizer and each prewashing device, also one of them prewashing device and thionizer can be combined, form the accumulation mode of communicating of top thionizer lower prewash device, by the compound mode of communicating that other prewashing devices and thionizer still adopt pipeline to be connected;
Methane steam reforming/CO changing device, described methane steam reforming/inlet mouth of CO changing device respectively with being communicated with of pressure-swing absorption apparatus and liquid nitrogen washing device, described methane steam reforming/air outlet of CO changing device is communicated with decarbonizing tower with pressure-swing absorption apparatus respectively, for by isolated for liquid nitrogen washing device CO and CH
4in cut and pressure-swing absorption apparatus, isolated resolution gas is recycled to methane steam reforming/CO changing device and transforms, the CO changed into
2and H
2, a part is returned to decarburization in the middle part of decarbonizing tower, and a part is delivered to pressure-swing absorption apparatus decarburization and carried hydrogen, decreases available gas H
2loss.
As a kind of preferred implementation, described thionizer is low-temperature rectisol thionizer, and described decarbonizing tower is low-temperature rectisol decarbonizing tower.
In order to make the mixed gas of different treatment amount obtain high-efficient purification, between described prewashing device and conversion refrigerating unit, or/and add flow control valve between described prewashing device and thionizer.
In addition, can also by the tower tray of former thionizer and prewashing device be replaced by CTST high-efficient solid mass transfer tower disc, strengthening methanol solution is to the absorption of sulfur-bearing component in mixed gas.
Mixed gas purification system of the present utility model, wet absorption purification has been carried out organic assembling with dry method pressure swing adsorption purge, according to the aperture of the amount adjustment prewashing device of pending mixed gas, thus reach the treatment capacity of adjustment desulfurization and decarburization, the coal gas treatment capacity of mixed gas purification system can be doubled, even several times, effectively improve mixed gas purification for H
2ability.When the amount of pending mixed gas exceedes the most load of prewashing device in system, only need add suitable prewashing device between conversion refrigerating unit and thionizer, without the need to changing follow-up equipment, avoid the second cover in parallel, even the huge investment of the three or four cover low-temperature rectisol and liquid nitrogen washing device.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the utility model embodiment.
In figure: 1. convert refrigerating unit, 2. prewashing device, 3. low-temperature rectisol thionizer, 4. low-temperature rectisol decarbonizing tower, 5. liquid nitrogen washing device, 6. pressure-swing absorption apparatus, 7. methane steam reforming/CO changing device.
Embodiment
In order to understand the utility model better, now explanation is further explained to the utility model in conjunction with the embodiments.
Mixed gas purification system as shown in Figure 1, comprise conversion refrigerating unit 1, two prewashing devices 2, low-temperature rectisol thionizer 3, low-temperature rectisol decarbonizing tower 4, liquid nitrogen washing device 5, pressure-swing absorption apparatus 6, methane steam reforming/CO changing device 7, the inlet mouth of two prewashing devices 2 is communicated with conversion refrigerating unit 1 respectively, the air outlet of two prewashing devices 2 is communicated with the inlet mouth of low-temperature rectisol thionizer 3, and two prewashing devices 2 and conversion refrigerating unit 1 between pipeline on add variable valve, the air outlet of low-temperature rectisol thionizer 3 is communicated with low-temperature rectisol decarbonizing tower 4 with pressure-swing absorption apparatus 6 respectively, low-temperature rectisol decarbonizing tower 4 is communicated with liquid nitrogen washing device 5, the resolution gas outlet of pressure-swing absorption apparatus 6 is communicated with methane steam reforming/CO changing device 7 respectively with the fraction outlets of liquid nitrogen washing device 5, methane steam reforming/CO changing device 7 air outlet is communicated with low-temperature rectisol decarbonizing tower 4 with pressure-swing absorption apparatus 6 respectively.
Concrete technological process is: the mixed gas after conversion carrying out transformation into itself's refrigerating unit is assigned to two prewashing devices and carries out the efficient de-oiling of prewashing, collect again and enter after low-temperature rectisol thionizer 3 carries out high-efficiency desulfurization, about 2/3 enters the decarburization of follow-up low-temperature rectisol decarbonizing tower 4, then delivers to CO and CH that liquid nitrogen washing device 5 removes trace
4, obtain pure hydrogen; Pressure-swing absorption apparatus 6 delivered to by the mixed gas of about 1/3, by different sorbent material successively selectively removing CO
2, CO, CH
4and rare gas element, obtain pure hydrogen.
By the CH that liquid nitrogen washing low temperature separation process goes out
4fraction becomes gas through re-heat, and after compressor pressurization, deliver to methane steam reforming/changing device 7, after transforming/converting, gas ingredients is mainly CO
2and H
2, about 3/5 is returned to decarburization in the middle part of low-temperature rectisol decarbonizing tower 4, and 2/5 delivers to pressure-swing absorption apparatus 6 decarburization carries hydrogen.
The original 300,000 tons/year of synthetic ammonia installations of certain group, the purification of ammonia synthesis gas adopts low-temperature rectisol desulfurization and decarburization, then removes after methane fraction and trace amounts of CO through liquid nitrogen washing deep cooling, joins nitrogen and obtain ammonia synthesis gas.After adopting above-mentioned mixed gas purification system, increase the treatment capacity of prewashing workshop section, make this system obtain H to mixed gas purification
2treatment capacity increase by 100%, do not need to change follow-up equipment, it is 600,000 tons/year that former 300,000 tons/year of synthetic ammonia installations can be made successfully to increase production.
Claims (3)
1. a mixed gas purification system, is characterized in that comprising:
Conversion refrigerating unit, for carrying out conversion cooling process by the mixed gas in device;
At least two prewashing devices, described prewashing device is communicated with conversion refrigerating unit, carries out pre-treatment for being assigned in each prewashing device by the part mixed gas through the process of conversion refrigerating unit;
Thionizer, the inlet mouth of described thionizer is communicated with each prewashing device, the air outlet of described thionizer is communicated with decarbonizing tower with pressure-swing absorption apparatus respectively, the air outlet of described decarbonizing tower is communicated with liquid nitrogen washing device, for carrying out desulfurization process by the gas collection in each prewashing device to thionizer, the gas after desulfurization being divided into two-way and carrying out purifying treatment and obtain hydrogen;
Methane steam reforming/CO changing device, described methane steam reforming/inlet mouth of CO changing device respectively with being communicated with of pressure-swing absorption apparatus and liquid nitrogen washing device, described methane steam reforming/air outlet of CO changing device is communicated with decarbonizing tower with pressure-swing absorption apparatus respectively, for by isolated for liquid nitrogen washing device CO and CH
4in cut and pressure-swing absorption apparatus, isolated resolution gas is recycled to methane steam reforming/CO changing device and transforms, the CO changed into
2and H
2, a part is returned to decarburization in the middle part of decarbonizing tower, and a part is delivered to pressure-swing absorption apparatus decarburization and carried hydrogen.
2. mixed gas purification system as claimed in claim 1, it is characterized in that: described thionizer is low-temperature rectisol thionizer, described decarbonizing tower is low-temperature rectisol decarbonizing tower.
3. mixed gas purification system as claimed in claim 1, is characterized in that: between described prewashing device and conversion refrigerating unit, or/and add flow control valve between described prewashing device and thionizer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520675943.4U CN204958384U (en) | 2015-09-02 | 2015-09-02 | Mix coal gas clean system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520675943.4U CN204958384U (en) | 2015-09-02 | 2015-09-02 | Mix coal gas clean system |
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|---|---|
| CN204958384U true CN204958384U (en) | 2016-01-13 |
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| CN201520675943.4U Active CN204958384U (en) | 2015-09-02 | 2015-09-02 | Mix coal gas clean system |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107213756A (en) * | 2017-06-15 | 2017-09-29 | 史汉祥 | A kind of flue gas purification system |
| CN107376618A (en) * | 2017-08-29 | 2017-11-24 | 华陆工程科技有限责任公司 | A kind of hydrogenation purification method of Sulfur Recovery Unit tail gas |
| CN112920859A (en) * | 2021-02-08 | 2021-06-08 | 赛鼎工程有限公司 | System and method for preparing methanol by deeply purifying coke oven gas |
-
2015
- 2015-09-02 CN CN201520675943.4U patent/CN204958384U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107213756A (en) * | 2017-06-15 | 2017-09-29 | 史汉祥 | A kind of flue gas purification system |
| CN107376618A (en) * | 2017-08-29 | 2017-11-24 | 华陆工程科技有限责任公司 | A kind of hydrogenation purification method of Sulfur Recovery Unit tail gas |
| CN112920859A (en) * | 2021-02-08 | 2021-06-08 | 赛鼎工程有限公司 | System and method for preparing methanol by deeply purifying coke oven gas |
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