CN216662494U - Pure hydrogen production synthetic ammonia system - Google Patents
Pure hydrogen production synthetic ammonia system Download PDFInfo
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- CN216662494U CN216662494U CN202123124001.1U CN202123124001U CN216662494U CN 216662494 U CN216662494 U CN 216662494U CN 202123124001 U CN202123124001 U CN 202123124001U CN 216662494 U CN216662494 U CN 216662494U
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Abstract
The utility model provides a system for producing synthetic ammonia by pure hydrogen, which belongs to the technical field of chemical product synthesis systems and comprises a deoxidizing tank, a first compression section, a second compression section, a desulfurizing tank and an ammonia synthesis device, wherein the deoxidizing tank is communicated with a nitrogen inlet pipe, the deoxidizing tank is communicated with the desulfurizing tank through the first compression section, the desulfurizing tank is communicated with a hydrogen inlet pipe, and the desulfurizing tank is communicated with the ammonia synthesis device through the second compression section. The utility model replaces coke oven gas in the prior art with pure hydrogen, and meets the requirements of safe production, environmental protection, production capacity and energy conservation through transformation and upgrading.
Description
Technical Field
The utility model belongs to the technical field of chemical product synthesis systems, and relates to a synthetic ammonia system, in particular to a system for producing synthetic ammonia by pure hydrogen.
Background
Referring to fig. 1, a synthetic ammonia co-production system in the prior art mainly uses coke oven gas and methanol purge gas as raw materials, coke oven gas from a gas holder is sequentially subjected to pressurization by a roots machine and temperature swing adsorption pretreatment for tar removal, benzene removal and desulfurization, hydrogen in the coke oven gas is extracted, the extracted hydrogen is compressed by a compressor and then mixed with the methanol purge gas, then the mixture enters the compressor for compression after pressure swing adsorption and hydrolysis hydrodesulfurization, methanol synthesis is performed after compression, hydrogen and nitrogen are compressed again for methanation, and the mixture enters a synthesis system for ammonia synthesis after methanation. The system mainly has the following defects in the ammonia synthesis process:
1. coke oven gas and methanol synthesis purge gas are used as raw materials, process gas purification is not thorough, the trace index of the process gas is high, namely, the trace of sulfur and the trace of oxygen both exceed standards, and the trace of sulfur is generally controlled to be less than 0.1ppm and the trace of oxygen is controlled to be less than 1 ppm.
2. The service life of the methanolizing copper-based catalyst in the system is 2 years, the service life of the methanation nickel-based catalyst is 4 years, the catalyst needs to be frequently replaced in the using process, and the two catalysts are expensive and have high production cost.
3. The ammonia synthesis pressure in the system is high, and the system resistance is large. The original ammonia synthesis internal part of the total quenching tower is designed under the working condition of high content of inert gases such as methanol, the operating pressure is 21-22Mpa, and the system resistance is 2-2.5 Mpa. High reaction temperature under high pressure, easy pulverization of the catalyst, short service life, few operation control means and great difficulty in safety management.
4. Low ammonia synthesis capacity and high production cost.
SUMMERY OF THE UTILITY MODEL
Aiming at the problems of incomplete process gas purification and high process gas trace index of the system for producing synthetic ammonia in the prior art, the utility model provides a system for producing synthetic ammonia by pure hydrogen. The system for producing synthetic ammonia by pure hydrogen does not need to extract hydrogen, and adds a deoxidizing tank and a desulfurizing tank, so that the trace of sulfur in the process gas is less than 0.1ppm and the trace of oxygen is less than 1ppm, and the specific technical scheme is as follows:
pure hydrogen production synthetic ammonia system, including deoxidation groove, first compression section, second compression section, desulfurization groove and ammonia synthesis device, the intercommunication has the nitrogen gas intake pipe on the deoxidation groove, the deoxidation groove is through first compression section and desulfurization groove intercommunication, the intercommunication has the hydrogen intake pipe on the desulfurization groove, the desulfurization groove passes through second compression section and ammonia synthesis device intercommunication.
Further inject, the synthetic ammonia system of pure hydrogen production still includes the hydrogen nitrogen blender, first compression section and hydrogen nitrogen blender intercommunication, the hydrogen intake pipe communicates with the hydrogen nitrogen blender, the hydrogen nitrogen blender is in proper order through desulfurization groove and second compression section and ammonia synthesizer intercommunication.
Further limited, the system for producing synthetic ammonia from pure hydrogen further comprises a make-up gas oil separator, and the second compression section is communicated with the ammonia synthesis device through the make-up gas oil separator.
Further, the system for producing synthetic ammonia from pure hydrogen further comprises an ammonia cooling device and an ammonia collecting device, wherein the ammonia collecting device is communicated with the ammonia synthesizing device through the ammonia cooling device.
Further limiting, the ammonia cooling device comprises a heat exchanger, a waste heat recoverer, a soft water heater, a synthesis water cooler and a cold exchanger, the air supply oil separator is communicated with the ammonia synthesis device through the heat exchanger, and the ammonia synthesis device is communicated with the ammonia collection device through the waste heat recoverer, the soft water heater, the heat exchanger, the synthesis water cooler and the cold exchanger in sequence.
Further, the ammonia cooling device further comprises an ammonia cooler and an ammonia separator, and the cold exchanger is communicated with the ammonia collecting device through the ammonia cooler and the ammonia separator in sequence.
Further defined, the ammonia cooling device further comprises a refrigeration system, and the ammonia cooler and the ammonia collection device are both communicated with the refrigeration system.
Further inject, refrigerating system includes third compression section, condenser and liquid ammonia storage tank, the cold ware of ammonia, third compression section, condenser, liquid ammonia storage tank and the cold ware of ammonia communicate in proper order after going to, liquid ammonia storage tank and ammonia collection device intercommunication.
Further defined, the pure hydrogen production synthetic ammonia system further comprises a circulator, and the cold exchanger is communicated with the heat exchanger through the circulator.
Further limited, an air separator is communicated with the nitrogen inlet pipe.
Compared with the prior art, the utility model has the beneficial effects that:
1. the system for producing synthetic ammonia by pure hydrogen comprises a deoxidizing tank, a first compression section, a second compression section, a desulfurizing tank and an ammonia synthesis device, wherein oxygen in nitrogen is removed by the deoxidizing tank, and sulfur in hydrogen is removed by the desulfurizing tank, so that the content of oxygen in nitrogen is less than 1ppm, and the content of sulfur in hydrogen is less than 0.1 ppm; the utility model eliminates the processes of pressurization, temperature swing adsorption, pressure swing adsorption and the like of the Roots machine, replaces the coke oven gas in the prior art with pure hydrogen, and meets the requirements of safe production, environmental protection, production capacity and energy conservation through transformation and upgrading.
2. According to the system for producing the synthetic ammonia by the pure hydrogen, the coke oven gas is replaced by the pure hydrogen, the methanol purge gas is replaced by the nitrogen, the hydrogen and the nitrogen are directly used as the raw materials for ammonia synthesis, a methanolized copper-based catalyst and a methanation nickel-based catalyst are not required to be used in the whole system, and the production cost is reduced.
3. The system for producing the synthetic ammonia by the pure hydrogen has the advantages that the operating pressure is less than 16Mpa, the system resistance is less than 2Mpa, the annual output is increased to 10-12 ten thousand tons from the previous 9 ten thousand tons, the ammonia synthesis capacity is improved, the safe production under the low-pressure operation is realized, and the economic benefit is maximized.
Drawings
FIG. 1 is a diagram of a prior art system for producing synthetic ammonia;
FIG. 2 is a diagram of a system for producing synthetic ammonia according to the present invention;
fig. 3 is a schematic diagram of a refrigeration system.
Detailed Description
The technical solutions of the present invention will be further explained below with reference to the drawings and examples, but the present invention is not limited to the embodiments described below.
The utility model relates to a system for producing synthetic ammonia by pure hydrogen, which comprises a deoxidizing tank, a first compression section, a second compression section, a desulfurizing tank and an ammonia synthesis device, wherein the deoxidizing tank is communicated with a nitrogen inlet pipe, the deoxidizing tank is communicated with the desulfurizing tank through the first compression section, the desulfurizing tank is communicated with a hydrogen inlet pipe, and the desulfurizing tank is communicated with the ammonia synthesis device through the second compression section. The synthetic ammonia system of pure hydrogen production still includes the hydrogen nitrogen blender, first compression section and hydrogen nitrogen blender intercommunication, hydrogen intake pipe and hydrogen nitrogen blender intercommunication, and the hydrogen nitrogen blender is through desulfurizing tank and second compression section and ammonia synthesizer intercommunication in proper order. The system for producing the synthetic ammonia by the pure hydrogen also comprises a make-up gas oil separator, and the second compression section is communicated with the ammonia synthesis device through the make-up gas oil separator. The system for producing the synthetic ammonia by the pure hydrogen further comprises an ammonia cooling device and an ammonia collecting device, and the ammonia collecting device is communicated with the ammonia synthesizing device through the ammonia cooling device. The ammonia cooling device comprises a heat exchanger, a waste heat recoverer, a soft water heater, a synthetic water cooler and a cold exchanger, the gas supplementing oil separator is communicated with the ammonia synthesis device through the heat exchanger, and the ammonia synthesis device is communicated with the ammonia collection device through the waste heat recoverer, the soft water heater, the heat exchanger, the synthetic water cooler and the cold exchanger in sequence. The ammonia cooling device also comprises an ammonia cooler and an ammonia separator, and the cold exchanger is communicated with the ammonia collecting device through the ammonia cooler and the ammonia separator in sequence. The ammonia cooling device also comprises a freezing system, and the ammonia cooler and the ammonia collecting device are communicated with the freezing system. The refrigerating system comprises a third compression section, a condenser and a liquid ammonia storage tank, an ammonia cooler, the third compression section, the condenser, the liquid ammonia storage tank and the ammonia cooler are sequentially communicated from front to back, and the liquid ammonia storage tank is communicated with an ammonia collecting device. The pure hydrogen production synthetic ammonia system also comprises a circulator, and the cold exchanger is communicated with the heat exchanger through the circulator. An air separator is communicated with the nitrogen inlet pipe.
Example 1
Referring to fig. 2, the system for producing synthetic ammonia from pure hydrogen in this embodiment includes a deoxidizing tank, a first compression section, a second compression section, a desulfurizing tank, a hydrogen-nitrogen mixer, an air-make-up oil separator, an ammonia synthesis device, and an ammonia collecting device, where the first compression section is a first compressor, the second compression section is a second compressor, the ammonia collecting device is a liquid ammonia spherical tank, the ammonia synthesis device is a synthesis tower, the deoxidizing tank is communicated with a nitrogen inlet pipe, the deoxidizing tank is communicated with the hydrogen-nitrogen mixer through the first compression section, the hydrogen-nitrogen mixer is communicated with a hydrogen inlet pipe, the hydrogen-nitrogen mixer is communicated with the desulfurizing tank, the desulfurizing tank is communicated with the second compression section, the second compression section is communicated with the air-make-up oil separator, and the air-make-up oil separator is communicated with the ammonia synthesis device.
The process for producing ammonia by the pure hydrogen production ammonia synthesis system comprises the following steps: introducing nitrogen into a deoxidation tank from a nitrogen inlet pipe, performing deoxidation treatment to reduce the content of oxygen to below 1ppm, compressing the oxygen-removed nitrogen in a first compressor, and compressing the nitrogen to 2.2 Mpa; pure hydrogen enters a hydrogen-nitrogen mixer to be uniformly mixed with nitrogen, the uniformly mixed nitrogen and hydrogen enter a desulfurization tank to be desulfurized, the pressure of the mixed gas of the nitrogen and the hydrogen which is discharged from the desulfurization tank is 2.1MPa, the mixed gas enters a second compression section to be compressed, the pressure of the mixed gas of the nitrogen and the hydrogen is compressed to be less than or equal to 16MPa, the mixed gas of the nitrogen and the hydrogen after being compressed enters an air supplementing oil separator, liquid such as oil, water and the like in the mixed gas of the nitrogen and the hydrogen is filtered and separated in the air supplementing oil separator, the mixed gas of the nitrogen and the hydrogen after being separated enters an ammonia synthesis device to be subjected to ammonia synthesis, the pressure of the mixed gas of the nitrogen and the hydrogen which enters the ammonia synthesis device is less than or equal to 16MPa, the pressure of the ammonia which is discharged from the ammonia synthesis device is 15.5MPa, and the temperature is 373 ℃.
Example 2
The system for producing synthetic ammonia from pure hydrogen comprises a deoxidizing tank, a first compression section, a second compression section, a desulfurizing tank, a hydrogen-nitrogen mixer, a make-up gas oil separator, an ammonia synthesis device, an ammonia cooling device, an ammonia collecting device, a circulator and an air separator, wherein the ammonia cooling device comprises a heat exchanger, a waste heat recoverer, a soft water heater, a synthetic water cooler, a cold exchanger, an ammonia cooler, an ammonia separator and a cooling system, referring to fig. 3, the cooling system comprises a third compression section, a condenser and a liquid ammonia storage tank, wherein the first compression section and the second compression section are integrated into a hydrogen-nitrogen combined compressor which is a hydrogen-nitrogen combined compressor disclosed in the patent CN209195623U published by the black cat coking corporation limited in shanxi, the third compression section is a third compressor, the ammonia collecting device is a liquid ammonia spherical tank, the ammonia synthesis device is a synthesis tower, the ammonia collecting device is a liquid ammonia spherical tank, the ammonia synthesizing device is a synthesizing tower, a nitrogen inlet pipe is communicated with a deoxidizing tank, the nitrogen inlet pipe is communicated with an air separator, the nitrogen in the air is separated out through the air separator, the deoxidizing tank is communicated with a hydrogen-nitrogen mixer through a first compression section, a hydrogen-nitrogen inlet pipe is communicated with the hydrogen-nitrogen mixer, the hydrogen-nitrogen mixer is communicated with a desulfurizing tank, the desulfurizing tank is communicated with a second compression section, the second compression section is communicated with an air-supplementing oil separator, the air-supplementing oil separator is communicated with the ammonia synthesizing device through a heat exchanger, the ammonia synthesizing device is communicated with a cold exchanger through the synthesizing tower, a waste heat recoverer, a soft water heater, a heat exchanger, a synthesizing cold water cooler and a cold exchanger in sequence, the ammonia cooler, a third compression section, a condenser, a liquid ammonia storage tank and the ammonia cooler are communicated in sequence from front to back, and the liquid ammonia storage tank is communicated with the ammonia collecting device, the ammonia cooler is communicated with the ammonia collecting device through an ammonia separator, the ammonia separator is communicated with the cold exchanger, and the cold exchanger is communicated with the heat exchanger through a circulator.
The process for producing ammonia by the pure hydrogen production ammonia synthesis system comprises the following steps: introducing nitrogen separated from air into a deoxidation tank through a nitrogen inlet pipe, performing deoxidation treatment to reduce the oxygen content to below 1ppm, compressing the nitrogen subjected to oxygen removal in a first compressor, and compressing the nitrogen to 2.2 MPa; pure hydrogen enters a hydrogen-nitrogen mixer to be uniformly mixed with nitrogen, the uniformly mixed nitrogen and hydrogen enter a desulfurizing tank to be desulfurized, the pressure of the mixed gas of the nitrogen and the hydrogen which is discharged from the desulfurizing tank is 2.1MPa, the mixed gas enters a second compression section to be compressed, the pressure of the mixed gas of the nitrogen and the hydrogen is compressed to be less than or equal to 16MPa, the mixed gas of the nitrogen and the hydrogen which is compressed enters an air-supplementing oil separator, liquid such as oil, water and the like in the mixed gas of the nitrogen and the hydrogen is filtered and separated by the air-supplementing oil separator, the pressure of the mixed gas of the nitrogen and the hydrogen which is separated is less than or equal to 16MPa and the temperature is 30 ℃, the mixed gas enters a heat exchanger, the mixed gas and ammonia which are discharged from a soft water heater are subjected to heat exchange in the heat exchanger and then are heated to raise the temperature to 140 ℃ and the pressure to be 16MPa, the mixed gas enters an ammonia synthesis device to be subjected to ammonia synthesis, the ammonia synthesis device, the pressure of the ammonia which is discharged from the ammonia synthesis device is 15.5MPa, the temperature is 373 ℃; ammonia enters a waste heat recoverer to exchange heat with water to reach a temperature of 200 ℃, then enters a soft water heater to exchange heat with water, the temperature is reduced to 175 ℃, ammonia coming out of the soft water heater enters a heat exchanger to exchange heat with a mixed gas of nitrogen and hydrogen coming out of a gas and oil separator, the temperature of the ammonia is reduced to 72 ℃, the ammonia coming out of the heat exchanger enters a synthetic water cooler to exchange heat with water in the synthetic water cooler, the temperature of the ammonia is reduced to 37 ℃, the ammonia coming out of a synthetic water cooler enters a cold exchanger, the ammonia in the cold exchanger exchanges heat with the mixed gas of nitrogen and hydrogen separated from an ammonia separator, the temperature of the ammonia is further reduced to 26 ℃, liquid ammonia coming out of the cold exchanger enters an ammonia collecting device to be collected, the ammonia coming out of the cold exchanger enters an ammonia cooler to be cooled, the temperature of the ammonia is reduced to-8 ℃, the ammonia coming out of the ammonia separator, the liquid ammonia separated from the ammonia separator enters an ammonia collecting device for collection, the mixed gas of nitrogen and hydrogen separated from the ammonia separator enters a cold exchanger, the mixed gas exchanges heat with ammonia coming out of a synthesis water cooler in the cold exchanger, the temperature is raised to 30 ℃, the mixed gas of the nitrogen and the hydrogen after temperature raising enters an ammonia synthesizing device for ammonia synthesis after heat exchange through a circulator.
The working process of the cooling system is as follows: the ammonia in the ammonia cooler exchanges heat with liquid ammonia (refrigerant) from a liquid ammonia storage tank, and the temperature of the ammonia in the ammonia cooler is reduced to-8 ℃ and then enters an ammonia separator; liquid ammonia (refrigerant) separated from a liquid ammonia storage tank is subjected to heat exchange in an ammonia cooler, the temperature of the liquid ammonia (refrigerant) is increased to 10 ℃ to form ammonia gas, the ammonia gas is compressed in a compressor, the temperature of the compressed ammonia gas is 70 ℃, the pressure of the compressed ammonia gas is 1.0MPa, then the compressed ammonia gas enters a condenser, the condenser is an evaporative condenser, the ammonia gas in the condenser is cooled, the temperature of the ammonia gas is reduced to 20 ℃ to form liquid ammonia, and the liquid ammonia enters a liquid ammonia storage tank for storage and convenient subsequent reutilization; the ammonia collection device supplements the liquid ammonia in the liquid ammonia storage tank.
Claims (10)
1. Pure hydrogen production synthetic ammonia system, its characterized in that, including deoxidation groove, first compression section, second compression section, desulfurization groove and ammonia synthesis device, the intercommunication has the nitrogen gas intake pipe on the deoxidation groove, the deoxidation groove is through first compression section and desulfurization groove intercommunication, the intercommunication has the hydrogen intake pipe on the desulfurization groove, the desulfurization groove passes through second compression section and ammonia synthesis device intercommunication.
2. The system for producing synthetic ammonia from pure hydrogen of claim 1, further comprising a hydrogen-nitrogen mixer, wherein the first compression section is in communication with the hydrogen-nitrogen mixer, wherein the hydrogen inlet pipe is in communication with the hydrogen-nitrogen mixer, and wherein the hydrogen-nitrogen mixer is in communication with the ammonia synthesis unit via the desulfurization tank and the second compression section in sequence.
3. The pure hydrogen ammonia production system of claim 2, further comprising a make-up oil separator, wherein the second compression stage is in communication with the ammonia synthesis unit via the make-up oil separator.
4. The pure hydrogen synthetic ammonia production system of claim 3 further comprising an ammonia cooling device and an ammonia collection device, wherein the ammonia collection device is in communication with the ammonia synthesis device via the ammonia cooling device.
5. The system for producing synthetic ammonia from pure hydrogen of claim 4, wherein the ammonia cooling device comprises a heat exchanger, a waste heat recoverer, a soft water heater, a synthetic water cooler, and a cold exchanger, the make-up air separator is in communication with the ammonia synthesis device through the heat exchanger, and the ammonia synthesis device is in communication with the ammonia collection device through the waste heat recoverer, the soft water heater, the heat exchanger, the synthetic water cooler, and the cold exchanger in this order.
6. The pure hydrogen ammonia production system of claim 5, wherein the ammonia cooling unit further comprises an ammonia cooler and an ammonia separator, and the cold exchanger is in communication with the ammonia collection unit through the ammonia cooler and the ammonia separator in sequence.
7. The pure hydrogen ammonia production system of claim 6, wherein the ammonia cooling device further comprises a refrigeration system, and wherein the ammonia cooler and the ammonia collection device are both in communication with the refrigeration system.
8. The system for producing synthetic ammonia from pure hydrogen of claim 7, wherein the refrigeration system comprises a third compression section, a condenser and a liquid ammonia storage tank, the ammonia cooler, the third compression section, the condenser, the liquid ammonia storage tank and the ammonia cooler are sequentially communicated from front to back, and the liquid ammonia storage tank is communicated with the ammonia collection device.
9. The pure hydrogen synthetic ammonia production system of claim 8 wherein the pure hydrogen synthetic ammonia production system further comprises a circulator, the cold exchanger being in communication with the heat exchanger via the circulator.
10. The system for producing synthetic ammonia from pure hydrogen of claim 9 wherein an air separator is connected to the nitrogen inlet line.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202123124001.1U CN216662494U (en) | 2021-12-13 | 2021-12-13 | Pure hydrogen production synthetic ammonia system |
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| CN202123124001.1U CN216662494U (en) | 2021-12-13 | 2021-12-13 | Pure hydrogen production synthetic ammonia system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114891546A (en) * | 2022-06-08 | 2022-08-12 | 佛燃能源集团股份有限公司 | System and method for preparing hydrogen and fuel-grade natural gas by using purge gas of synthetic ammonia |
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2021
- 2021-12-13 CN CN202123124001.1U patent/CN216662494U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114891546A (en) * | 2022-06-08 | 2022-08-12 | 佛燃能源集团股份有限公司 | System and method for preparing hydrogen and fuel-grade natural gas by using purge gas of synthetic ammonia |
| CN114891546B (en) * | 2022-06-08 | 2022-12-09 | 佛燃能源集团股份有限公司 | System and method for preparing hydrogen and fuel-grade natural gas by using purge gas of synthetic ammonia |
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