CN102491270A - Purification device and purification method for ammonia synthesis raw material gas - Google Patents
Purification device and purification method for ammonia synthesis raw material gas Download PDFInfo
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Abstract
The invention relates to the field of raw material gas purification in the ammonia synthesis production process and discloses a purification device and a purification method for ammonia synthesis raw material gas. The device comprises a pre-cooling heat exchanger, a copious-cooling heat exchanger, a demethanizing tower and a methane recovering tower, wherein the ammonia synthesis raw material gas is sequentially connected with the pre-cooling heat exchanger, the copious-cooling heat exchanger, the demethanizing tower and the methane recovering tower through pipelines, synthesis gas with the hydrogen-to-nitrogen mixture ratio being 3:1 is obtained at the tower top of the demethanizing tower, and products are obtained at the tower bottom of the methane recovering tower. The purification device and the purification method have the advantages that the problem of too high exhausted gas emission quantity of ammonia synthesis plants adopting the methanation process can be solved, and simultaneously, products can be obtained.
Description
Technical field
The present invention relates to the field of purification of virgin gas in the Ammonia Production technology, relate in particular to a kind of refining plant and purifying method of syngas for synthetic ammonia.
Background technology
In synthetic ammonia installation, synthesis gas purification is an important process link.Traditional technical process is that virgin gas gets into compressed element after primary reformer conversion, secondary reformer conversion, CO conversion, methanation, drying, in the high pressure synthesis unit, carries out building-up reactions then and generates synthetic ammonia.
Owing to contain a small amount of methane and argon gas through in the pretreated virgin gas; And these a spot of methane and argon gas are not participated in reaction in ammonia synthesis reaction; Thereby just having increasing methane and argon gas accumulation, the result causes the dividing potential drop of nitrogen and hydrogen to reduce, and influences speed of reaction and transformation efficiency.Therefore after methane and argon gas are accumulated to finite concentration, reaction gas is discharged.So just cause the loss of a large amount of hydrogen, reduced the yield of product.Adopt deep cooling Blang technology can methane in the virgin gas and argon gas major part be removed, thereby reduced the accumulation of rare gas element in the reactors for synthesis of ammonia, improved hydrogen partial pressure, increased the yield of product.
Yet methane in Blang's technology in the virgin gas and nitrogen, argon gas bleed off as tail gas together, do not obtain reclaiming.And energy shortage at present, therefore the recovery to methane in the virgin gas just seems particularly important.
Summary of the invention
The purpose of this invention is to provide a kind of quantity discharged that synthetic ammonia factory speeds to exit that reduced, improved productive rate, reduced energy consumption, reclaimed the refining plant and the purifying method thereof of the syngas for synthetic ammonia of methane in the virgin gas simultaneously.
In order to solve the problems of the technologies described above, the present invention is able to solve through following technical proposals:
A kind of refining plant of syngas for synthetic ammonia; Comprise precool heat exchanger device, deep cooling interchanger, demethanizing tower, synthetic ammonia feedstock air pipe and nitrogen pipeline; The synthetic ammonia feedstock air pipe links to each other with precool heat exchanger device, deep cooling interchanger, demethanizing tower successively; Nitrogen pipeline links to each other with precool heat exchanger device, deep cooling interchanger, demethanizing tower successively, and said refining plant also comprises the methane recovery tower, and the methane recovery tower links to each other with at the bottom of the demethanizer through pipeline.
As preferably, the refining plant of described syngas for synthetic ammonia also comprises the nitrogen expansion machine, and the import of nitrogen expansion machine links to each other with the nitrogen pipeline that is arranged on precool heat exchanger device middle part, and the nitrogen expansion machine exports and links to each other with the low-pressure nitrogen export pipeline of deep cooling interchanger.
As preferably; The refining plant of described syngas for synthetic ammonia also comprises the circulating nitrogen gas compressor; The circulating nitrogen gas compressor inlet links to each other with the low-pressure nitrogen export pipeline of precool heat exchanger device, and the circulating nitrogen gas compressor outlet links to each other with the high pressure nitrogen inlet ductwork of precool heat exchanger device.
The present invention also provides a kind of purifying method of syngas for synthetic ammonia, comprises the steps:
A, with syngas for synthetic ammonia successively through entering into demethanizing tower after precool heat exchanger device, the exchange of deep cooling exchanger heat, above-mentioned raw materials gas is removed most of methane and argon gas in demethanizing tower, and ejects synthetic gas hydrogen and nitrogen from its rectifying tower;
Still liquid in b, the demethanizing tower is through getting into the methane recovery tower behind the expenditure and pressure;
Through after precool heat exchanger device, the exchange of deep cooling exchanger heat, expenditure and pressure gets in demethanizer column overhead condensing surface and the methane recovery column overhead condensing surface high pressure nitrogen that c, circulating nitrogen gas compressor produce respectively successively;
The nitrogen that evaporates in d, demethanizer column overhead condensing surface and the methane recovery column overhead condensing surface passes through deep cooling interchanger, precool heat exchanger device respectively, gets into the circulating nitrogen gas compressor after the re-heat, returns the precool heat exchanger device again after supercharging and the cooling, forms the nitrogen refrigeration cycle;
Step e: high pressure nitrogen is extracted one out at precool heat exchanger device middle part, gets into nitrogen expansion machine swell refrigeration, and the back nitrogen that expands is back in the deep cooling interchanger low-pressure nitrogen export pipeline.
As preferably, the described synthetic gas hydrogen that ejects from rectifying tower and the volume ratio of nitrogen are 3:1.
As preferably, the working pressure in the described methane recovery tower is 200 ~ 800KPaG.
As preferably, the high pressure nitrogen among the described step c is-100 ~-140 ℃ through the cooled temperature of precool heat exchanger device, is-170 ~-190 ℃ through the cooled temperature of deep cooling interchanger.
As preferably, the high pressure nitrogen among the described step e is 30 ~ 80 ℃ through the cooled temperature of precool heat exchanger device.
The present invention has significant technique effect owing to adopted above technical scheme:
1, the present invention has reduced the quantity discharged that synthetic ammonia factory speeds to exit effectively, gain in yield, and energy consumption reduces.
2, reclaim the methane in the virgin gas, can be used as product LNG and sell, increased the output value.
Description of drawings
Fig. 1 is a structural representation of the present invention.
Fig. 2 is a principle of work synoptic diagram of the present invention.
Embodiment
The present invention is described in further detail with embodiment below in conjunction with accompanying drawing 1 to accompanying drawing 2:
Embodiment 1
The refining plant of syngas for synthetic ammonia; As depicted in figs. 1 and 2; Comprise precool heat exchanger device 1, deep cooling interchanger 2, demethanizing tower 4, synthetic ammonia feedstock air pipe 101 and nitrogen pipeline 201; Synthetic ammonia feedstock air pipe 101 links to each other with precool heat exchanger device 1, deep cooling interchanger 2, demethanizing tower 4 successively; Nitrogen pipeline 201 links to each other with precool heat exchanger device 1, deep cooling interchanger 2, demethanizing tower 4 successively, and said refining plant also comprises the methane recovery tower, and the methane recovery tower links to each other with at the bottom of demethanizing tower 4 towers through pipeline.
This refining plant also comprises nitrogen expansion machine 3, and 3 imports of nitrogen expansion machine link to each other with the nitrogen pipeline 202 that is arranged on precool heat exchanger device 1 middle part, and 3 outlets of nitrogen expansion machine link to each other with the low-pressure nitrogen export pipeline 203 of deep cooling interchanger 2.
This refining plant also comprises circulating nitrogen gas compressor 6, and 6 imports of circulating nitrogen gas compressor link to each other with the low-pressure nitrogen export pipeline 102 of precool heat exchanger device 1, and 6 outlets of circulating nitrogen gas compressor link to each other with the high pressure nitrogen inlet ductwork 103 of precool heat exchanger device 1.
The purifying method of syngas for synthetic ammonia, as shown in Figure 2, method is following:
Virgin gas after the methanation; Cool to-125 ℃ through precool heat exchanger device 1; And then process deep cooling interchanger 2 is cooled to-180 ℃; Get into demethanizing tower 4, virgin gas is removed most of methane and argon gas in demethanizing tower 4, and the synthetic gas hydrogen and the nitrogen volume ratio of going out from rectifying tower top reach 3:1.4 ends of demethanizing tower, be mainly the mixing liquid of nitrogen, methane and argon, behind expenditure and pressure, gets into methane recovery tower 5.Working pressure 350KPaG in the methane recovery tower 5 obtains purity and is 98% liquid methane at the bottom of the tower, cat head is mainly nitrogen and small quantity of hydrogen and argon gas.The cat head low-temperature receiver of demethanizing tower 4 and methane recovery tower 5 provides through the nitrogen refrigeration cycle; High pressure nitrogen is from nitrogen compressor 6; Be cooled to-50 ℃ through precool heat exchanger device 1, a part is extracted into decompressor 3 out from precool heat exchanger device 1 middle part, and the nitrogen after expanding through the nitrogen expansion machine is back to low-pressure nitrogen export pipeline 203; Another part goes out precool heat exchanger device 1 after continuing to be cooled to-125 ℃, continues to be cooled to-179 ℃ at deep cooling interchanger 2 then.Get in the overhead condenser of demethanizing tower 4 and methane recovery tower 5 after being divided into the other throttling of two stocks then; The evaporation and the low temperature cold is provided in the overhead condenser of demethanizing tower 4 and methane recovery tower 5 of low pressure liquid nitrogen; Nitrogen after the evaporation merges entering low-pressure nitrogen pipeline after going out condenser/evaporator respectively; Be back to 2 re-heats of deep cooling interchanger, the nitrogen after low-pressure nitrogen goes out deep cooling interchanger 2 backs and expands through decompressor mixes the back and gets into precool heat exchanger device 1, and re-heat is to normal temperature.After low-pressure nitrogen after the re-heat is pressurized to 3500KPaG through circulating nitrogen gas compressor 6, returns precool heat exchanger device 1 again and continue cooling, in system, move in circles like this, for system provides cold.
In a word, the above is merely preferred embodiment of the present invention, and all equalizations of doing according to claim of the present invention change and modify, and all should belong to the covering scope of patent of the present invention.
Claims (8)
1. the refining plant of a syngas for synthetic ammonia; Comprise precool heat exchanger device (1), deep cooling interchanger (2), demethanizing tower (4), synthetic ammonia feedstock air pipe (101) and nitrogen pipeline (201); It is characterized in that: described synthetic ammonia feedstock air pipe (101) links to each other with precool heat exchanger device (1), deep cooling interchanger (2), demethanizing tower (4) successively; Nitrogen pipeline (201) links to each other with precool heat exchanger device (1), deep cooling interchanger (2), demethanizing tower (4) successively; Said refining plant also comprises methane recovery tower (5), and methane recovery tower (5) links to each other with at the bottom of demethanizing tower (4) tower through pipeline.
2. the refining plant of syngas for synthetic ammonia according to claim 1; It is characterized in that: also comprise nitrogen expansion machine (3); Nitrogen expansion machine (3) import links to each other with the nitrogen pipeline (202) that is arranged on precool heat exchanger device (1) middle part, and nitrogen expansion machine (3) outlet links to each other with the low-pressure nitrogen export pipeline (203) of deep cooling interchanger (2).
3. the refining plant of syngas for synthetic ammonia according to claim 1; It is characterized in that: also comprise circulating nitrogen gas compressor (6); Circulating nitrogen gas compressor (6) import links to each other with the low-pressure nitrogen export pipeline (102) of precool heat exchanger device (1), and circulating nitrogen gas compressor (6) outlet links to each other with the high pressure nitrogen inlet ductwork (103) of precool heat exchanger device (1).
4. the purifying method of a syngas for synthetic ammonia is characterized in that, comprises the steps:
A, enter into demethanizing tower after syngas for synthetic ammonia passed through precool heat exchanger device (1), deep cooling interchanger (2) heat exchange successively; Above-mentioned raw materials gas is removed most of methane and argon gas in demethanizing tower (4), and ejects synthetic gas hydrogen and nitrogen from its rectifying tower;
Still liquid in b, the demethanizing tower (4) is through getting into methane recovery tower (5) behind the expenditure and pressure;
After the high pressure nitrogen that c, circulating nitrogen gas compressor (6) produce passed through precool heat exchanger device (1), deep cooling interchanger (2) heat exchange successively, expenditure and pressure got in demethanizing tower (4) overhead condenser (41) and methane recovery tower (5) overhead condenser (51) respectively;
The nitrogen of evaporation in d, demethanizing tower (4) overhead condenser (41) and methane recovery tower (5) overhead condenser (51); Pass through deep cooling interchanger (2), precool heat exchanger device (1) respectively; Get into circulating nitrogen gas compressor (6) after the re-heat; Return precool heat exchanger device (1) again after supercharging and the cooling, form the nitrogen refrigeration cycle;
E: high pressure nitrogen is extracted one out at precool heat exchanger device (1) middle part, gets into nitrogen expansion machine (3) swell refrigeration, and the back nitrogen that expands is back in deep cooling interchanger (2) the low-pressure nitrogen export pipeline (203).
5. the purifying method of syngas for synthetic ammonia according to claim 4 is characterized in that: the described synthetic gas hydrogen that ejects from rectifying tower and the volume ratio of nitrogen are 3:1.
6. according to the purifying method of the described syngas for synthetic ammonia of claim 4, it is characterized in that: the working pressure in the described methane recovery tower (5) is 200 ~ 800KPaG.
7. the purifying method of syngas for synthetic ammonia according to claim 4; It is characterized in that: the high pressure nitrogen among the described step c is-100 ~-140 ℃ through the cooled temperature of precool heat exchanger device (1), is-170 ~-190 ℃ through the cooled temperature of deep cooling interchanger (2).
8. the purifying method of syngas for synthetic ammonia according to claim 4 is characterized in that: the high pressure nitrogen among the described step e is 30 ~ 80 ℃ through the cooled temperature of precool heat exchanger device (1).
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| CN103213946A (en) * | 2013-04-23 | 2013-07-24 | 江苏中核华纬工程设计研究有限公司 | Method for synthesizing ammonia by comprehensively utilizing liquefied natural gas |
| CN106369934A (en) * | 2016-10-25 | 2017-02-01 | 杭州中泰深冷技术股份有限公司 | Frozen blocking preventing co-production LNG liquid nitrogen wash device combined with mixed refrigerant system and method thereof |
| CN111634883A (en) * | 2020-05-29 | 2020-09-08 | 西安陕鼓动力股份有限公司 | Pretreatment method and system for synthesis ammonia raw material gas |
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| CN103213946A (en) * | 2013-04-23 | 2013-07-24 | 江苏中核华纬工程设计研究有限公司 | Method for synthesizing ammonia by comprehensively utilizing liquefied natural gas |
| CN103213946B (en) * | 2013-04-23 | 2015-02-18 | 江苏中核华纬工程设计研究有限公司 | Method for synthesizing ammonia by comprehensively utilizing liquefied natural gas |
| CN106369934A (en) * | 2016-10-25 | 2017-02-01 | 杭州中泰深冷技术股份有限公司 | Frozen blocking preventing co-production LNG liquid nitrogen wash device combined with mixed refrigerant system and method thereof |
| CN106369934B (en) * | 2016-10-25 | 2022-04-26 | 杭州中泰深冷技术股份有限公司 | Anti-freezing and anti-blocking co-production LNG liquid nitrogen washing device and method combined with mixed refrigerant system |
| CN111634883A (en) * | 2020-05-29 | 2020-09-08 | 西安陕鼓动力股份有限公司 | Pretreatment method and system for synthesis ammonia raw material gas |
| CN111634883B (en) * | 2020-05-29 | 2024-05-28 | 西安陕鼓动力股份有限公司 | Pretreatment method and system for synthesis ammonia feed gas |
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