CN204752197U - Synthetic ammonia synthetic gas self -loopa cryogenic separation purifier - Google Patents
Synthetic ammonia synthetic gas self -loopa cryogenic separation purifier Download PDFInfo
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- CN204752197U CN204752197U CN201520436412.XU CN201520436412U CN204752197U CN 204752197 U CN204752197 U CN 204752197U CN 201520436412 U CN201520436412 U CN 201520436412U CN 204752197 U CN204752197 U CN 204752197U
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Abstract
The utility model discloses a synthetic ammonia synthetic gas self -loopa cryogenic separation purifier. The device includes that cryrogenic heat exchanger, rich hydrogen scrubbing tower, demethanation take off argon column, compressor, first expander, second expander, first cooler, second cooler, third cooler, first choke valve, second choke valve, third choke valve, synthetic ammonia feed gas pipeline, nitrogen hydrogen circulation pipeline and liquefied gas pipeline, the demethanation take off the inside reboiler that is equipped with at the bottom of the argon column tower, adopt the utility model discloses the synthetic ammonia feed gas of cryogenic purification can obtain high -purity nitrogen hydrogen than being close to for 1 at rich hydrogen scrubbing tower top of the tower: 3 the synthetic gas, can obtain the liquefied natural gas product at the bottom of the argon column tower is taken off in the demethanation, the utility model provides a traditional methanation technology speed exit the emission big, retrieve shortcoming, the high scheduling problem of running cost, realized need not outside extra high -pressure nitrogen gas circulation refrigeration, reduce the energy consumption, when promoting operation purification efficiency, guarantee the recycle of methane in the feed gas.
Description
Technical field
The utility model relates to chemical industry cryogenic purification device, particularly relates to a kind of synthetic ammonia synthetic gas self-circulation low temperature separation process refining plant.
Background technology
In synthetic ammonia technical development process, research mainly concentrates on and reduces energy consumption and improve in energy efficiency.There is a large amount of medium and small synthetic ammonia installations in China at present in operation.The technical process of this kind of synthetic ammonia installation mainly comprises that unstripped gas compression, unstripped gas desulfurization, primary reformer conversion, secondary reformer conversion, CO conversion, CO2 absorption, methanation, synthetic gas are dry, synthetic gas compression, ammonia synthesis and the workshop section such as freezing.Cryogenic purification technique is that the synthetic gas compressed by synthetic gas is extracted out, and by the technique of cryogenic purification, methane wherein and excessive argon are taken out, the nitrogen hydrogen after purification returns synthetic gas press.
Owing to containing a small amount of methane and argon gas in pretreated unstripped gas, and these a small amount of methane and argon gas do not participate in reaction in ammonia synthesis reaction, thus just have increasing methane and argon gas accumulation, this all can have disadvantageous effect to molecular balance, progress and energy consumption.Therefore, after methane and argon gas are accumulated to finite concentration, reaction gas be discharged.So just cause the loss of a large amount of hydrogen, reduce the yield of product.Adopt cryogenic purification technique can to remove in unstripped gas almost all methane, most of argon gas and excessive nitrogen, thus reduce the accumulation of rare gas element in reactors for synthesis of ammonia, improve hydrogen partial pressure, add the yield of product.
Methane in current ammonia synthesis process Raw gas bleeds off as tail gas together with nitrogen, argon gas, is not recycled.Wherein methane is as renewable energy source, and produce annual nearly 1,000,000 yuan of the methane slatterned as gas of ceasing to be binding of ten thousand tons of synthesis ammonia plants per year through budget, global energy is nervous especially at present, therefore just seems particularly important to the recovery of methane in unstripped gas.
Invention disclosed patent before my company: a kind of refining plant of syngas for synthetic ammonia and purifying method, ZL201110386815.4, although solve blast expense of ceasing to be binding to a certain extent, but its whole device needs to provide low-temperature receiver by high pressure nitrogen circularly cooling, its high pressure nitrogen derives from external process, need extra high cost to run, calculate with 300kt/a synthesis ammonia system, year needs nearly 1,800 ten thousand yuan of the extra electricity charge.
Summary of the invention
The purpose of this utility model overcomes the deficiencies in the prior art, provides a kind of synthetic ammonia synthetic gas self-circulation low temperature separation process refining plant.
A kind of synthetic ammonia synthetic gas self-circulation low temperature separation process refining plant, comprise deep-cooling heat exchanger, rich hydrogen washing tower, demethanizing take off argon column, compressor, the first decompressor, the second decompressor, the first water cooler, the second water cooler, the 3rd water cooler, first throttle valve, second throttle, the 3rd throttling valve, synthetic ammonia feedstock air pipe, nitrogen hydrogen circulation line and liquefied gas pipeline, described demethanizing takes off inside at the bottom of argon column tower and comprises reboiler;
Synthetic ammonia feedstock air pipe is connected with rich hydrogen washing tower bottom through deep-cooling heat exchanger, and rich hydrogen wash tower bottoms is passed through liquefied gas pipeline and is connected with first throttle valve, and continues across deep-cooling heat exchanger and take off argon column bottom with demethanizing and be connected; Demethanizing takes off argon column top by nitrogen hydrogen circulation line, is connected successively through deep-cooling heat exchanger with compressor, the first water cooler;
First cooler outlet is divided into upper and lower road, set out on a journey and bifurcation stream, wherein one flows through nitrogen hydrogen circulation line, be connected with the first expander end through deep-cooling heat exchanger, first expander brings out mouth through deep-cooling heat exchanger in the middle, and the nitrogen hydrogen circulation line taking off argon column top with demethanizing is connected to form and confluxes; Another flows through nitrogen hydrogen circulation line, is connected successively with the first decompressor pressurized end, the second water cooler, the second decompressor pressurized end, the 3rd water cooler;
3rd cooler outlet is by nitrogen hydrogen circulation line, also two tributaries are again divided in the middle through deep-cooling heat exchanger, wherein a tributary is connected with the second expander end, and the second expander brings out nitrogen hydrogen circulation line that mouth and demethanizing take off argon column top and is connected to form and confluxes; The reboiler that another tributary and demethanizing take off inside at the bottom of argon column tower is connected;
The reboiler outlet that demethanizing takes off inside at the bottom of argon column tower is divided into two tributaries again by nitrogen hydrogen circulation line, and wherein a tributary is connected with second throttle, rich hydrogen washing tower top successively; Another tributary takes off argon column top with the 3rd throttling valve, demethanizing successively and is connected.
As preferably, under described rich hydrogen washing tower top and the first cooler outlet, road is formed and confluxes, then synthesizes compression set with nitrogen hydrogen and be connected.
As preferably, described demethanizing takes off the liquefied gas pipeline bottom argon column, is connected with natural gas liquids collection device through deep-cooling heat exchanger.
As preferably, described demethanizing takes off in the middle part of argon column and is connected with argon-rich gas collection device.
Adopt the utility model, effectively reduce Blang's ammonia synthesis process energy consumption, improve cryogenic purification efficiency, decrease the quantity discharged of synthetic ammonia factory periodic off-gases, add synthetic ammonia feedstock productive rate, whole cryogenic purification flow process is flexible, convenient, stable.Syngas for synthetic ammonia is by after the process of the utility model cryogenic purification, high-purity nitrogen hydrogen is obtained than the synthetic gas being close to 1:3 at rich hydrogen washing tower tower top, take off at the bottom of argon column tower in demethanizing and obtain liquefied natural gas product, produce ten thousand tons of synthesis ammonia plants per year through budget and can collect natural gas liquids every year and just can realize 1,000,000 yuan of economic benefits; Simultaneously the utility model run needed for low-temperature receiver be directed to the rich nitrogen that syngas for synthetic ammonia separates and carry out circularly cooling, without the need to outside additional high pressure nitrogen circulation refrigeration, calculate with 300kt/a synthesis ammonia system, year can save nearly 1,800 ten thousand yuan of the extra electricity charge, effectively alleviates social energy shortage.
Accompanying drawing explanation
Fig. 1 is synthetic ammonia synthetic gas self-circulation low temperature separation process refining plant schematic diagram;
Fig. 2 is synthetic ammonia synthetic gas self-circulation low temperature separation process purifying method schematic diagram;
In figure, deep-cooling heat exchanger 1, rich hydrogen washing tower 2, demethanizing take off argon column 3, compressor 4, first decompressor 5, second decompressor 6, first water cooler 7, second water cooler 8, the 3rd water cooler 9, first throttle valve 10, second throttle 11, the 3rd throttling valve 12, reboiler 13.
Embodiment
As shown in Figure 1, a kind of synthetic ammonia synthetic gas self-circulation low temperature separation process refining plant, comprise deep-cooling heat exchanger 1, rich hydrogen washing tower 2, demethanizing take off argon column 3, compressor 4, first decompressor 5, second decompressor 6, first water cooler 7, second water cooler 8, the 3rd water cooler 9, first throttle valve 10, second throttle 11, the 3rd throttling valve 12, synthetic ammonia feedstock air pipe, nitrogen hydrogen circulation line and and liquefied gas pipeline, described demethanizing takes off inside at the bottom of argon column 3 tower and is provided with reboiler 13;
Synthetic ammonia feedstock air pipe is connected with rich hydrogen washing tower 2 bottom through deep-cooling heat exchanger 1, is connected bottom rich hydrogen washing tower 2 by liquefied gas pipeline with first throttle valve 10, and continues across deep-cooling heat exchanger 1 and take off argon column 3 bottom with demethanizing and be connected; Demethanizing takes off argon column 3 top by nitrogen hydrogen circulation line, is connected successively through deep-cooling heat exchanger 1 with compressor 4, first water cooler 7;
First water cooler 7 outlet is divided into upper and lower road, set out on a journey and bifurcation stream, wherein one flows through nitrogen hydrogen circulation line, be connected with the first decompressor 5 expanding end through deep-cooling heat exchanger 1, first decompressor 5 expanding end outlet is through deep-cooling heat exchanger 1 in the middle, and the nitrogen hydrogen circulation line taking off argon column 3 top with demethanizing is connected to form and confluxes; Another flows through nitrogen hydrogen circulation line, is connected successively with the first decompressor 5 pressurized end, the second water cooler 8, second decompressor 6 pressurized end, the 3rd water cooler 9;
3rd water cooler 9 exports by nitrogen hydrogen circulation line, also two tributaries are again divided in the middle through deep-cooling heat exchanger 1, wherein a tributary is connected with the second decompressor 6 expanding end, and the nitrogen hydrogen circulation line that the second decompressor 6 expanding end outlet and demethanizing take off argon column 3 top is connected to form and confluxes; The reboiler 13 that another tributary and demethanizing take off inside at the bottom of argon column 3 tower is connected;
The reboiler 13 that demethanizing takes off inside at the bottom of argon column 3 tower exports and is again divided into two tributaries by nitrogen hydrogen circulation line, and wherein a tributary is connected with second throttle 11, rich hydrogen washing tower 2 top successively; Another tributary takes off argon column 3 top with the 3rd throttling valve 12, demethanizing successively and is connected.
Described rich hydrogen washing tower 2 top and the first water cooler 7 export lower road and are formed and conflux, then synthesize compression set with nitrogen hydrogen and be connected.
Described demethanizing takes off the liquefied gas pipeline bottom argon column 3, is connected with natural gas liquids collection device through deep-cooling heat exchanger 1.
Described demethanizing takes off in the middle part of argon column 3 and is connected with argon-rich gas collection device.
As shown in Figure 2, a kind of cryogenic purification method of synthetic ammonia synthetic gas self-circulation low temperature separation process refining plant comprises the following steps:
1) syngas for synthetic ammonia a enters into rich hydrogen washing tower 2 bottom after deep-cooling heat exchanger 1 heat exchange, top-down low temperature liquid rich nitrogen hydrogen b carries out gas-liquid two-phase counter current contact generation interphase mass transfer with top from bottom to top, thus obtain rich hydrogen gas mixture c at rich hydrogen washing tower 2 tower top, its hydrogen, nitrogen mol ratio are 3.0 ~ 3.2:1, without argon gas, methane, rich hydrogen gas mixture c transfers to nitrogen hydrogen synthesis compression set and carries out ammonia synthesis reaction after deep-cooling heat exchanger 1 heat exchange; At the bottom of rich hydrogen washing tower 2 tower, obtain still liquid d, its hydrogen, nitrogen, argon gas, methane mol ratio are 1:20 ~ 23:0.9 ~ 1:13 ~ 16;
2) still liquid d is by after first throttle valve 10 expenditure and pressure, after deep-cooling heat exchanger 1 heat exchange, enter into demethanizing take off argon column 3 and carry out gas-liquid two-phase counter current contact generation interphase mass transfer with the top-down low temperature liquid in top rich nitrogen hydrogen b, thus take off argon column 3 tower top in demethanizing and obtain rich nitrogen mixed gas e, its hydrogen, nitrogen mol ratio are 1:19 ~ 22, without argon gas, methane; Take off argon column 3 centre exit in demethanizing and obtain argon-rich gas; Take off at the bottom of argon column 3 tower in demethanizing and obtain natural gas liquids, and after deep-cooling heat exchanger 1 heat exchange, transfer to natural gas liquids collection device collect;
3) rich nitrogen mixed gas e, first the rich nitrogen mixed gas exported with the second decompressor 6 expanding end converges, then the rich nitrogen mixed gas also exported with the first decompressor 5 expanding end in the middle through deep-cooling heat exchanger 1 converges, after deep-cooling heat exchanger 1 heat exchange, compress through compressor 4 successively, after the first water cooler 7 cools, wherein part rich hydrogen gas mixture enters lower road pipeline and rich hydrogen gas mixture c and converges and transfer to nitrogen hydrogen and synthesize compression set and carry out ammonia synthesis reaction;
4) the rich nitrogen mixed gas e of another part enters pipeline of setting out on a journey and is divided into two tributaries, a wherein tributary f, expand through deep-cooling heat exchanger 1 heat exchange, the first decompressor 5 expanding end successively, again through deep-cooling heat exchanger 1 also in the middle, take off argon column 3 top rich nitrogen mixed gas e out with demethanizing and converge formation partial circulating;
5) another tributary g compresses through the first decompressor 5 pressurized end successively, the second water cooler 8 cools, the second decompressor 6 pressurized end compresses and after the 3rd water cooler 9 cooling process, through deep-cooling heat exchanger 1 heat exchange, and be divided into again two tributaries in the middle; After wherein a tributary h is delivered to the second decompressor 6 expanding end expansion process, takes off argon column 3 top rich nitrogen mixed gas e out with demethanizing and converge formation systemic circulation;
6) another tributary h is delivered to the reboiler 13 that demethanizing takes off inside at the bottom of argon column 3 tower, after reboiler 13 vaporization process, again be divided into two tributaries, wherein a tributary i is through second throttle 11, enter rich hydrogen washing tower 2 tower top to wash syngas for synthetic ammonia a, another tributary j after the 3rd throttling valve 12 expenditure and pressure, enter demethanizing take off argon column 3 tower top to vaporization still liquid d wash.
Synthetic ammonia synthetic gas self-circulation low temperature separation process purifying method, the described methane working pressure taken off in argon column 3 tower is 410 ~ 490KPaG; In step 5) successively through the first decompressor 5 pressurized end compression, the second water cooler 8 cools, tributary g after the second decompressor 6 pressurized end compression and the 3rd water cooler 9 cooling process, through deep-cooling heat exchanger 1 heat exchange, rich nitrogen mixed gas e temperature is in the middle-105 ~-135 DEG C; Enter the tributary g of reboiler 13 in step 6), its inner rich nitrogen mixed gas e temperature is-175 ~-185 DEG C.
Claims (4)
1. a synthetic ammonia synthetic gas self-circulation low temperature separation process refining plant, it is characterized in that comprising deep-cooling heat exchanger (1), rich hydrogen washing tower (2), demethanizing takes off argon column (3), compressor (4), first decompressor (5), second decompressor (6), first water cooler (7), second water cooler (8), 3rd water cooler (9), first throttle valve (10), second throttle (11), 3rd throttling valve (12), synthetic ammonia feedstock air pipe, nitrogen hydrogen circulation line and liquefied gas pipeline, described demethanizing takes off inside at the bottom of argon column (3) tower and is provided with reboiler (13),
Synthetic ammonia feedstock air pipe is connected with rich hydrogen washing tower (2) bottom through deep-cooling heat exchanger (1), rich hydrogen washing tower (2) bottom is connected with first throttle valve (10) by liquefied gas pipeline, and continues across deep-cooling heat exchanger (1) and take off argon column (3) bottom with demethanizing and be connected; Demethanizing takes off argon column (3) top by nitrogen hydrogen circulation line, is connected successively through deep-cooling heat exchanger (1) with compressor (4), the first water cooler (7);
First water cooler (7) outlet is divided into upper and lower road, set out on a journey and bifurcation stream, wherein one flows through nitrogen hydrogen circulation line, be connected with the first decompressor (5) expanding end through deep-cooling heat exchanger (1), through deep-cooling heat exchanger (1) and in the middle, the nitrogen hydrogen circulation line taking off argon column (3) top with demethanizing is connected to form and confluxes the outlet of first decompressor (5) expanding end; Another flows through nitrogen hydrogen circulation line, is connected successively with the first decompressor (5) pressurized end, the second water cooler (8), the second decompressor (6) pressurized end, the 3rd water cooler (9);
3rd water cooler (9) outlet is by nitrogen hydrogen circulation line, again be divided into two tributaries in the middle through deep-cooling heat exchanger (1), wherein a tributary is connected with the second decompressor (6) expanding end, and the nitrogen hydrogen circulation line that the outlet of the second decompressor (6) expanding end and demethanizing take off argon column (3) top is connected to form and confluxes; The reboiler (13) that another tributary and demethanizing take off inside at the bottom of argon column (3) tower is connected;
Reboiler (13) outlet that demethanizing takes off inside at the bottom of argon column (3) tower is divided into two tributaries again by nitrogen hydrogen circulation line, and wherein a tributary is connected with second throttle (11), rich hydrogen washing tower (2) top successively; Another tributary takes off argon column (3) top with the 3rd throttling valve (12), demethanizing successively and is connected.
2. synthetic ammonia synthetic gas self-circulation low temperature separation process refining plant according to claim 1, is characterized in that described rich hydrogen washing tower (2) top and the first water cooler (7) export lower road and formed and conflux, then synthesizes compression set with nitrogen hydrogen and be connected.
3. synthetic ammonia synthetic gas self-circulation low temperature separation process refining plant according to claim 1, is characterized in that described demethanizing takes off the liquefied gas pipeline of argon column (3) bottom, is connected through deep-cooling heat exchanger (1) with natural gas liquids collection device.
4. synthetic ammonia synthetic gas self-circulation low temperature separation process refining plant according to claim 1, is characterized in that described demethanizing takes off argon column (3) middle part and is connected with argon-rich gas collection device.
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| CN201520436412.XU CN204752197U (en) | 2015-06-24 | 2015-06-24 | Synthetic ammonia synthetic gas self -loopa cryogenic separation purifier |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104986734A (en) * | 2015-06-24 | 2015-10-21 | 杭州中泰深冷技术股份有限公司 | Synthesis ammonia and synthesis gas self-circulation cryogenic separation purifying device and purifying 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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2015
- 2015-06-24 CN CN201520436412.XU patent/CN204752197U/en not_active Withdrawn - After Issue
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104986734A (en) * | 2015-06-24 | 2015-10-21 | 杭州中泰深冷技术股份有限公司 | Synthesis ammonia and synthesis gas self-circulation cryogenic separation purifying device and purifying 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 |
| 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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Legal Events
| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20151111 Effective date of abandoning: 20171114 |