Metal cracking hydrogen production device of ammonia synthesis system

Abstract

The utility model discloses a metal cracking hydrogen production device of a synthetic ammonia system, which comprises a synthetic ammonia steam inlet and a cracking reactor, and water steam enters the cracking reactor and then is subjected to catalytic reduction reaction in the cracking reactor to generate mixed gas of hydrogen and water steam; and a condenser and a gas-liquid separator. Treating the mixed gas of hydrogen and water vapor to obtain hydrogen and condensed water; the device further comprises a transfer tank, hydrogen enters the transfer tank to be stored, and condensate water is output and collected through a pipeline. And the transfer tank is provided with two process systems, namely a synthetic ammonia section and a liquid hydrogen production section. According to the hydrogen production device, hydrogen is used for replacing a synthetic ammonia coal gasification hydrogen production process, so that the problem of carbon dioxide emission in the synthetic ammonia coal gasification hydrogen production process can be solved; and 2, the purification process of the crude feed gas of the original synthetic ammonia coal gasification hydrogen can be simplified, including desulfurization, transformation, decarbonization, refining and other processes, and the shortening of the production process can obviously reduce the production cost and reduce the energy consumption.

Description

Technical Field

[0001] The utility model relates to the technical field of new energy synthetic ammonia hydrogen production process, in particular to a synthetic ammonia system metal cracking hydrogen production device. Background Art

[0002] As a renewable, clean and efficient secondary energy source, hydrogen energy has many advantages such as abundant resources, wide sources, high combustion calorific value, clean and pollution-free, diverse utilization forms, can be used as an energy storage medium and good safety. It is an important energy source for achieving energy transformation and carbon neutrality.

[0003] At present, synthetic ammonia systems mostly use synthetic gas as the source, but synthetic gas cannot be compared with hydrogen. It is an industry trend to add hydrogen production system to the synthetic ammonia system. It can replace the synthetic gas source and develop a new industrial chain of liquid hydrogen and hydrogen reactors, which is in line with the current direction of social energy development.

[0004] Therefore, based on the above technical problems, technicians in this field urgently need to develop a metal cracking hydrogen production device for a synthetic ammonia system. Utility Model Content

[0005] The utility model aims to provide a metal cracking hydrogen production device for a synthetic ammonia system, which can achieve an annual reduction of carbon dioxide emissions of more than 3000t.

[0006] In order to achieve the above purpose, the utility model provides the following technical solutions:

[0007] The utility model discloses a metal cracking hydrogen production device for a synthetic ammonia system, which comprises:

[0008] A synthetic ammonia steam inlet, which is connected to the gas-making boiler at the upstream end of the process through a pipeline, and the water vapor generated by the gas-making boiler at the upstream end of the process enters the synthetic ammonia steam inlet;

[0009] A cracking reactor connected to the synthetic ammonia steam inlet, wherein the water vapor enters the cracking reactor and undergoes a catalytic reduction reaction in the cracking reactor to generate a mixed gas of hydrogen and water vapor;

[0010] A condenser and a gas-liquid separator are sequentially arranged at the downstream end of the cracking reactor process;

[0011] The mixed gas of hydrogen and water vapor is processed in turn by the condenser and the gas-liquid separator to obtain hydrogen and condensed water;

[0012] The device also includes a transfer tank located at the downstream end of the gas-liquid separator process, hydrogen enters the transfer tank for storage, and condensed water is output and collected through a pipeline;

[0013] The downstream process end of the transfer tank has two process systems, namely, a synthetic ammonia section and a liquid hydrogen production section.

[0014] Furthermore, the condenser is provided with a circulating cooling water loop;

[0015] The circulating cooling water loop is divided into a circulating cooling water inlet loop and a circulating cooling water outlet loop;

[0016] The circulating cooling water inlet circuit is connected to the lower part of the condenser, and the circulating cooling water outlet circuit is connected to the upper part of the condenser.

[0017] Furthermore, the water vapor generated by the gasification boiler at the upstream end of the process is used as the gas source of the hydrogen production device, and the water vapor generated by the gasification boiler is reduced in pressure by a pressure reducing valve to control the pressure at 0.6MPa-1.0MPa;

[0018] Before the water vapor enters the cracking reactor, it is decompressed to 0.3MPa-0.4MPa by a pressure reducing valve, and the pressure inside the cracking reactor is 0.65MPa-0.7MPa, and the pressure holding time is 20min-30min.

[0019] Furthermore, the cracking reactor contains a catalyst.

[0020] Furthermore, the pressure in the transfer tank is maintained at 0.2MPa-0.3MPa.

[0021] Furthermore, the transfer tank transports the produced hydrogen to the synthetic hydrogen and nitrogen compressor, and after increasing the pressure to 14MPa-20MPa, it is transported to the synthetic ammonia section to produce ammonia.

[0022] Furthermore, the transfer tank transports the produced hydrogen to the synthetic hydrogen compressor, and liquefies it after pressurization to produce liquid hydrogen.

[0023] In the above technical scheme, the utility model provides a metal cracking hydrogen production device for a synthetic ammonia system, which has the following beneficial effects:

[0024] The hydrogen production device of the utility model uses hydrogen to replace the synthetic ammonia coal gasification hydrogen production process. Firstly, it can solve the carbon dioxide emission problem in the synthetic ammonia coal gasification hydrogen production process; secondly, it can simplify the raw material gas purification process of the original synthetic ammonia coal gasification hydrogen, including desulfurization, conversion, decarbonization, refining and other processes. The shortening of the production process can significantly reduce production costs and reduce energy consumption. BRIEF DESCRIPTION OF THE DRAWINGS

[0025] In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, the drawings required for use in the embodiments will be briefly introduced below. It is obvious that the drawings described below are only some embodiments recorded in the present utility model. For ordinary technicians in this field, other drawings can also be obtained based on these drawings.

[0026] Figure 1 The present invention discloses a process flow chart of a metal cracking hydrogen production device in a synthetic ammonia system.

[0027] Description of reference numerals:

[0028] 1. Synthetic ammonia steam inlet; 2. Cracking reactor; 3. Condenser; 4. Gas-liquid separator; 5. Transfer tank; 6. Circulating cooling water inlet loop; 7. Circulating cooling water outlet loop; 8. Synthetic hydrogen and nitrogen compressor; 9. Synthetic hydrogen compressor; 10. Condensate collection; 11. Circulating cooling water loop. DETAILED DESCRIPTION

[0029] In order to enable those skilled in the art to better understand the technical solution of the present invention, the present invention will be further described in detail below in conjunction with the accompanying drawings.

[0030] See also Figure 1 As shown;

[0031] A metal cracking hydrogen production device for a synthetic ammonia system according to the present embodiment comprises:

[0032] A synthetic ammonia steam inlet 1, which is connected to the gas-making boiler at the upstream end of the process through a pipeline, and the water vapor generated by the gas-making boiler at the upstream end of the process enters the synthetic ammonia steam inlet 1;

[0033] A cracking reactor 2 connected to the synthetic ammonia steam inlet 1, after the water vapor enters the cracking reactor 2, a catalytic reduction reaction is carried out in the cracking reactor 2 to produce a mixed gas of hydrogen and water vapor;

[0034] A condenser 3 and a gas-liquid separator 4 are sequentially arranged at the process downstream end of the cracking reactor 2;

[0035] The mixed gas of hydrogen and water vapor is processed in turn by the condenser 3 and the gas-liquid separator 4 to obtain hydrogen and condensed water;

[0036] The device also includes a transfer tank 5 located at the downstream end of the gas-liquid separator 4, hydrogen enters the transfer tank 5 for storage, and condensed water is output and collected through a pipeline;

[0037] The downstream end of the transfer tank 5 has two process systems, namely, the synthetic ammonia section and the liquid hydrogen production section.

[0038] The hydrogen production device disclosed in this embodiment uses water vapor as a raw material, and the water vapor generated by the gasification boiler is decompressed by a pressure reducing valve and then transported to the cracking reactor 2 downstream of the process. After that, the water vapor passes through a reaction system containing a catalyst to produce a mixed gas of hydrogen and water vapor through a catalytic reduction reaction. Then, the gas and liquid are separated in turn through a condenser 3 and a gas-liquid separator 4 to obtain hydrogen with a purity of 99%, and the obtained qualified hydrogen is transported to the downstream of the process through a pipeline.

[0039] Preferably, the condenser 3 of this embodiment is provided with a circulating cooling water loop 11;

[0040] The circulating cooling water loop 11 is divided into a circulating cooling water inlet loop 6 and a circulating cooling water outlet loop 7;

[0041] The circulating cooling water inlet loop 6 is connected to the lower part of the condenser 3 , and the circulating cooling water outlet loop 7 is connected to the upper part of the condenser 3 .

[0042] The water vapor generated by the gasification boiler at the upstream end of the process is used as the gas source of the hydrogen production device, and the water vapor generated by the gasification boiler is reduced in pressure through a pressure reducing valve to control the pressure at 0.6MPa-1.0MPa;

[0043] Before the water vapor enters the cracking reactor 2, it is decompressed to 0.3MPa-0.4MPa by a pressure reducing valve, and the pressure inside the cracking reactor 2 is 0.65MPa-0.7MPa, and the pressure holding time is 20min-30min.

[0044] The cracking reactor 2 of this embodiment has a catalyst. The catalyst of this embodiment is mainly aluminum, including aluminum and aluminum alloys, iron and iron alloys, etc. The problem of low activity at low temperature is solved; aluminum cracking agents are first reduced when used, so that metal elements such as aluminum play the role of active components in the form of metal; aluminum oxide is used as a carrier to play a dispersing role; zinc oxide plays a stabilizing role, which solves the problems of too fast or too slow reaction, and can stably produce a mixed gas of hydrogen and water vapor.

[0045] Preferably, the pressure in the transfer tank 5 of this embodiment is maintained at 0.2MPa-0.3MPa.

[0046] Preferably, the transfer tank 5 of this embodiment transports the produced hydrogen to the synthetic hydrogen and nitrogen compressor 8, and after the pressure is increased to 14MPa-20MPa, it is transported to the synthetic ammonia section to produce ammonia.

[0047] The specific process flow is that the cracking reactor 2 uses 155°C and 0.6MPa water vapor as raw material, and enters the cracking reactor after being decompressed to 0.3MPa-0.4MPa, so that the pressure in the cracking reactor 2 reaches 0.65MPa-0.7MPa, and the pressure is maintained for 20min-30min. The water vapor and the cracking agent catalyst react to generate a mixed gas of hydrogen and water vapor. After that, the product produced by the cracking reactor 2 enters the transfer tank 5 through the condenser 3 and the gas-liquid separator 4. Observe the pressure gauge of the transfer tank 5, wait for its pressure to slowly rise to 0.4MPa, open and adjust the outlet valve of the transfer tank 5, and maintain its pressure between 0.2MPa-0.3MPa. At this time, the product hydrogen concentration is 99% and the temperature is 40°C. The obtained product hydrogen is sent to the synthetic hydrogen nitrogen compressor 8, the pressure is increased to 14MPa-20MPa, and sent to the synthetic ammonia section to produce ammonia; the second is sent to the synthetic hydrogen compressor 9, and liquefied after pressurization to produce liquid hydrogen.

[0048] Specifically, the transfer tank 5 transports the produced hydrogen to the synthetic hydrogen compressor 9, and liquefies it after pressurization to produce liquid hydrogen.

[0049] In addition, the chemical reaction equations involved during the implementation of the synthetic ammonia system of this embodiment are as follows:

[0050] 2Al+6H2O=(heating)2Al(OH)3+3H2↑

[0051] N2(g)+3H2(g)=(high temperature, high pressure, catalyst)2NH3(g)

[0052] In the above technical scheme, the utility model provides a metal cracking hydrogen production device for a synthetic ammonia system, which has the following beneficial effects:

[0053] The hydrogen production device of the utility model uses hydrogen to replace the synthetic ammonia coal gasification hydrogen production process. Firstly, it can solve the carbon dioxide emission problem in the synthetic ammonia coal gasification hydrogen production process; secondly, it can simplify the raw material gas purification process of the original synthetic ammonia coal gasification hydrogen, including desulfurization, conversion, decarbonization, refining and other processes. The shortening of the production process can significantly reduce production costs and reduce energy consumption.

[0054] The above only describes some exemplary embodiments of the present invention by way of illustration. It is undoubted that those skilled in the art can modify the described embodiments in various ways without departing from the spirit and scope of the present invention. Therefore, the above drawings and descriptions are illustrative in nature and should not be construed as limiting the scope of protection of the claims of the present invention.

Claims

1. A metal cracking hydrogen production device for a synthetic ammonia system, characterized in that: The device includes: A synthetic ammonia steam inlet (1), the synthetic ammonia steam inlet (1) is connected to the gas-making boiler at the upstream end of the process through a pipeline, and water vapor generated by the gas-making boiler at the upstream end of the process enters the synthetic ammonia steam inlet (1); A cracking reactor (2) connected to the synthetic ammonia steam inlet (1), wherein the water vapor enters the cracking reactor (2) and undergoes a catalytic reduction reaction in the cracking reactor (2) to generate a mixed gas of hydrogen and water vapor; A condenser (3) and a gas-liquid separator (4) are sequentially arranged at the process downstream end of the cracking reactor (2); The mixed gas of hydrogen and water vapor is processed in turn by the condenser (3) and the gas-liquid separator (4) to obtain hydrogen and condensed water; The device also includes a transfer tank (5) located at the process downstream end of the gas-liquid separator (4), hydrogen enters the transfer tank (5) for storage, and condensed water is output through a pipeline and collected; The process downstream end of the transfer tank (5) has two process systems, namely, a synthetic ammonia section and a liquid hydrogen production section.

2. The metal cracking hydrogen production device for ammonia synthesis system according to claim 1, characterized in that: The condenser (3) is provided with a circulating cooling water loop (11); The circulating cooling water loop (11) is divided into a circulating cooling water inlet loop (6) and a circulating cooling water outlet loop (7); The circulating cooling water inlet circuit (6) is connected to the lower part of the condenser (3), and the circulating cooling water outlet circuit (7) is connected to the upper part of the condenser (3).

3. The metal cracking hydrogen production device for ammonia synthesis system according to claim 1, characterized in that: The water vapor generated by the gasification boiler at the upstream end of the process is used as the gas source of the hydrogen production device, and the water vapor generated by the gasification boiler is reduced in pressure through a pressure reducing valve to control the pressure within 0.6MPa-1.0MPa; Before the water vapor enters the cracking reactor (2), it is decompressed to 0.3MPa-0.4MPa by a pressure reducing valve, and the pressure inside the cracking reactor is 0.65MPa-0.7MPa, and the pressure holding time is 20min-30min.

4. The metal cracking hydrogen production device for ammonia synthesis system according to claim 3, characterized in that: The cleavage reactor (2) contains a catalyst.

5. The metal cracking hydrogen production device for ammonia synthesis system according to claim 1, characterized in that: The pressure in the transfer tank (5) is maintained at 0.2MPa-0.3MPa.

6. The metal cracking hydrogen production device for ammonia synthesis system according to claim 1, characterized in that: The transfer tank (5) transports the produced hydrogen to the synthetic hydrogen and nitrogen compressor (8), and after the pressure is increased to 14 MPa-20 MPa, it is transported to the synthetic ammonia section to produce ammonia.

7. The metal cracking hydrogen production device for ammonia synthesis system according to claim 1, characterized in that: The transfer tank (5) transports the produced hydrogen to the synthetic hydrogen compressor (9), and liquefies the hydrogen after pressurization to produce liquid hydrogen.

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