CN202379728U - Device for purifying synthesis ammonia raw material gas - Google Patents
Device for purifying synthesis ammonia raw material gas Download PDFInfo
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- CN202379728U CN202379728U CN2011204843249U CN201120484324U CN202379728U CN 202379728 U CN202379728 U CN 202379728U CN 2011204843249 U CN2011204843249 U CN 2011204843249U CN 201120484324 U CN201120484324 U CN 201120484324U CN 202379728 U CN202379728 U CN 202379728U
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Abstract
The utility model relates to the field of the purification of raw material gas in a process for producing synthesis ammonia, and discloses a device for purifying synthesis ammonia raw material gas. The device comprises a precooling heat exchanger, a deep cooling heat exchanger, a demethanizer and a methane recovery tower, wherein the synthesis ammonia raw material gas is connected with the precooling heat exchanger, the deep cooling heat exchanger, the demethanizer and the methane recovery tower sequentially by a pipeline; synthesis gas of hydrogen and nitrogen in a ratio of 3:1 is obtained on the top of the demethanizer; and products are obtained at the bottom of the methane recovery tower. By the device, the problem of large discharge amount of purge gas in synthesis ammonia factories applying a methanation process is solved, and the products can be obtained simultaneously.
Description
Technical field
The utility model relates to the field of purification of virgin gas in the Ammonia Production technology, relates in particular to a kind of refining plant 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 the utility model provides a kind of quantity discharged that synthetic ammonia factory speeds to exit that reduces, and has improved productive rate, has reduced energy consumption, has reclaimed the refining plant 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 utility model 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 purifying method of the utility model 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 utility model has significant technique effect owing to adopted above technical scheme:
1, the utility model has reduced the quantity discharged that synthetic ammonia factory speeds to exit effectively, gain in yield, and energy consumption reduces.
2, the methane in the recyclable virgin gas of the utility model can be used as product LNG and sells, and has increased the output value.
Description of drawings
Fig. 1 is the structural representation of the utility model.
Fig. 2 is the principle of work synoptic diagram of the utility model.
Embodiment
The utility model 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 the preferred embodiment of the utility model, and all equalizations of being done according to the utility model claim change and modify, and all should belong to the covering scope of the utility model patent.
Claims (3)
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).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011204843249U CN202379728U (en) | 2011-11-29 | 2011-11-29 | Device for purifying synthesis ammonia raw material gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011204843249U CN202379728U (en) | 2011-11-29 | 2011-11-29 | Device for purifying synthesis ammonia raw material gas |
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| Publication Number | Publication Date |
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| CN202379728U true CN202379728U (en) | 2012-08-15 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN2011204843249U Expired - Lifetime CN202379728U (en) | 2011-11-29 | 2011-11-29 | Device for purifying synthesis ammonia raw material gas |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102491270A (en) * | 2011-11-29 | 2012-06-13 | 杭州中泰深冷技术股份有限公司 | Purification device and purification method for ammonia synthesis raw material gas |
| CN109612203A (en) * | 2018-11-22 | 2019-04-12 | 山东润银生物化工股份有限公司 | A kind of processing method of discharge gas in ammonia synthesis |
-
2011
- 2011-11-29 CN CN2011204843249U patent/CN202379728U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102491270A (en) * | 2011-11-29 | 2012-06-13 | 杭州中泰深冷技术股份有限公司 | Purification device and purification method for ammonia synthesis raw material gas |
| CN102491270B (en) * | 2011-11-29 | 2013-07-10 | 杭州中泰深冷技术股份有限公司 | Purification device and purification method for ammonia synthesis raw material gas |
| CN109612203A (en) * | 2018-11-22 | 2019-04-12 | 山东润银生物化工股份有限公司 | A kind of processing method of discharge gas in ammonia synthesis |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20120815 |