CN116239083A - Low-temperature conversion structure for synthesizing ammonia by hydrocarbon steam conversion method - Google Patents

Low-temperature conversion structure for synthesizing ammonia by hydrocarbon steam conversion method Download PDF

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Publication number
CN116239083A
CN116239083A CN202310218281.7A CN202310218281A CN116239083A CN 116239083 A CN116239083 A CN 116239083A CN 202310218281 A CN202310218281 A CN 202310218281A CN 116239083 A CN116239083 A CN 116239083A
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China
Prior art keywords
low
temperature shift
tank
temperature
desulfurization
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CN202310218281.7A
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李明
白文斌
陈满元
赵之斌
陈立南
诸兵
钟家旺
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China BlueChemical Ltd
CNOOC Fudao Ltd
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China BlueChemical Ltd
CNOOC Fudao Ltd
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Priority to CN202310218281.7A priority Critical patent/CN116239083A/en
Publication of CN116239083A publication Critical patent/CN116239083A/en
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
    • C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
    • C01B3/16—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
    • C01B2203/0288—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step containing two CO-shift steps
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/068—Ammonia synthesis
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1041—Composition of the catalyst
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1041—Composition of the catalyst
    • C01B2203/1047—Group VIII metal catalysts
    • C01B2203/1052—Nickel or cobalt catalysts
    • C01B2203/1058—Nickel catalysts
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Industrial Gases (AREA)

Abstract

The invention discloses a low-temperature conversion structure for synthesizing ammonia by a hydrocarbon steam conversion method. The invention structurally comprises a desulfurization unit, a hydrogenation reactor, a low-temperature conversion unit, a high-temperature conversion unit and a front-mounted detoxification tank of a low-temperature conversion furnace; the low-temperature shift converter is internally filled with detoxication agent in a front detoxication tank; the low-temperature shift converter front-end detoxification tank is arranged in a line between the high-temperature shift unit and the low-temperature shift unit through a pipeline and is used for removing low-temperature shift catalyst poison brought into the low-temperature shift unit by a previous procedure; the desulfurization unit comprises a common desulfurization tank and a standby desulfurization tank; the installation position of the front detoxification tank of the low-temperature shift converter is positioned at the installation position of any common desulfurization tank or standby desulfurization tank. According to the invention, the spare idle desulfurization tank is changed into the additional detoxification tank in front of the low-temperature shift converter for use, so that the low-temperature shift catalyst poison brought by the previous working procedure is removed while the desulfurization effect is not influenced, the service life of the catalyst is prolonged, and the forced shutdown caused by the replacement of the low-temperature shift catalyst is reduced.

Description

Low-temperature conversion structure for synthesizing ammonia by hydrocarbon steam conversion method
Technical Field
The invention belongs to the technical field of ammonia synthesis equipment, and relates to a low-temperature conversion structure for synthesizing ammonia by a hydrocarbon steam conversion method.
Background
The classical hydrocarbon steam conversion process for synthesizing ammonia is equipped with carbon monoxide conversion section. The carbon monoxide conversion section is further divided into a high temperature conversion unit and a low temperature conversion unit. Copper-based catalysts are generally used for the low-temperature shift unit. Copper-based catalysts are susceptible to reaction with sulfur-containing and chlorine-containing compounds, which results in catalyst poisoning and loss of catalytic activity. Usually, the shutdown overhaul time of the ammonia synthesis system is 2-3 years, but because the service life of the low-temperature change catalyst is affected by the use condition and uncertainty exists, the catalyst is often required to be replaced by the low-temperature change unit, so that the whole device is forced to be shut down in advance, and the production time is lost.
The new factory can adopt a mode of connecting small low-temperature furnaces in series or setting larger low-temperature furnaces to improve the service time of the low-temperature conversion unit, but for the in-service factory, because of compact equipment arrangement, the new low-temperature furnaces are basically not constructed in site if the new low-temperature furnaces are connected in series or in parallel.
Disclosure of Invention
The invention aims to provide a low-temperature conversion structure for synthesizing ammonia by a hydrocarbon steam conversion method. The invention can replace the spare desulfurization tank with the desulfurizing agent serving as the detoxification agent as the front-mounted detoxification tank of the low-temperature shift converter through the pipeline, the front-mounted detoxification tank of the low-temperature shift converter is connected with the low-temperature shift converter in series, the front-mounted detoxification tank of the low-temperature shift converter is used for removing the low-temperature shift catalyst poison brought by the previous working procedure, the service life of the low-temperature shift catalyst is prolonged, the service life of the low-temperature shift catalyst is ensured, and the forced shutdown caused by replacing the low-temperature shift catalyst in the low-temperature shift converter is reduced.
The invention provides a low-temperature conversion structure for synthesizing ammonia by a hydrocarbon steam conversion method, which comprises a desulfurization unit, a hydrogenation reactor, a low-temperature conversion unit and a high-temperature conversion unit, and is characterized by further comprising a front detoxification tank of a low-temperature conversion furnace;
the low-temperature shift converter is internally filled with detoxication agent in a front-mounted detoxication tank; the low-temperature shift converter front-end detoxification tank is arranged in a line between the high-temperature shift unit and the low-temperature shift unit through a pipeline and is used for removing low-temperature shift catalyst poison brought into the low-temperature shift unit by a previous procedure;
the desulfurization unit comprises a common desulfurization tank and a standby desulfurization tank; the installation position of the front detoxification tank of the low-temperature shift converter is positioned at the installation position of any one of the common desulfurization tank or the standby desulfurization tank.
In the low-temperature conversion structure for synthesizing ammonia by the hydrocarbon steam conversion method, the front detoxification tank of the low-temperature conversion furnace is the standby desulfurization tank for removing the desulfurizing agent and separating from the desulfurization unit.
In the low-temperature conversion structure for synthesizing ammonia by using the hydrocarbon steam conversion method, the low-temperature conversion unit comprises a low-temperature conversion furnace, and the high-temperature conversion unit comprises a high-temperature conversion furnace;
the bottom of the front detoxification tank of the low-temperature shift converter is connected with the top of the low-temperature shift converter through a pipeline to form a series structure;
the top of the front detoxification tank of the low-temperature shift converter is connected with the lower part of the high-temperature shift converter through a pipeline to form a series structure;
the bottom of the hydrogenation reactor is connected with the top of the common desulfurization tank through a pipeline to form a series structure.
In the low-temperature conversion structure for synthesizing ammonia by the hydrocarbon steam conversion method, the front detoxification tank of the low-temperature conversion furnace, the common desulfurization tank, the hydrogenation reactor, the low-temperature conversion furnace and the high-temperature conversion furnace are arranged in a row in sequence.
In the low-temperature conversion structure for synthesizing ammonia by the hydrocarbon steam conversion method, the detoxication agent comprises a desulfurizing agent and/or a dechlorinating agent; the desulfurizing agent and/or dechlorinating agent are employed by the industry.
The invention has the following technical effects:
according to the invention, a low-temperature conversion structure for preparing synthetic ammonia by a hydrocarbon steam conversion method can be realized, and in one implementation manner, the structure can comprise a low-temperature conversion furnace front-end detoxification tank, wherein the interior of the low-temperature conversion furnace front-end detoxification tank is used for filling a low-temperature conversion catalyst detoxification agent, and the low-temperature conversion catalyst detoxification agent comprises a dechlorination agent and/or a desulfurizing agent; the front detoxification tank of the additional low-temperature conversion furnace is arranged in the line of the original low-temperature conversion unit through a pipeline; wherein, the installation position of the front detoxification tank of the low-temperature shift converter is positioned at the installation position of any desulfurization tank of the original desulfurization unit. According to the low-temperature conversion catalyst detoxification agent, the spare desulfurization tank which is idle is used as the front-end detoxification tank of the additional low-temperature conversion furnace, the desulfurization agent in the spare desulfurization tank can be replaced by the low-temperature conversion catalyst detoxification agent when the desulfurization effect is not affected, the low-temperature conversion catalyst detoxification agent comprises a dechlorination agent and/or a desulfurization agent, low-temperature conversion catalyst poison brought in by a pre-process is removed, the service life of the catalyst is prolonged, the service life of the low-temperature conversion unit is further prolonged, the operation period of the device is prolonged, and the production stopping time of the device is shortened.
Drawings
The accompanying drawings are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate the invention and together with the embodiments of the invention, serve to explain the invention. In the drawings:
FIG. 1 is a schematic diagram of connection of a low-temperature shift structure for synthesizing ammonia by a hydrocarbon steam conversion method according to an embodiment of the present invention;
FIG. 2 is a schematic diagram of the connection of a desulfurization unit and a low temperature shift unit arrangement in a classical ammonia synthesis process.
The individual labels in the figures are as follows:
a 108DC low-temperature shift converter front-end detoxification tank; 108DC1 standby desulfurization tank; 108DB commonly used desulfurization tanks; 108DA hydrogenation reactor; 104D2 low temperature shift furnace; 104D1 high temperature shift furnace.
Detailed Description
In order to facilitate the understanding of the present technical solution, a preferred embodiment of the present invention will be described below with reference to the accompanying drawings, it being understood that the preferred embodiment described herein is for the purpose of illustrating and explaining the present invention only and is not to be construed as limiting the present invention.
Examples
FIG. 1 shows a schematic connection of a low-temperature conversion structure for synthesizing ammonia by a hydrocarbon steam conversion method according to an embodiment of the present invention. The structure comprises a low-temperature shift converter front-end detoxification tank 108DC, a desulfurization unit, a hydrogenation reactor 108DA, a low-temperature shift unit and a high-temperature shift unit. The low temperature shift unit includes a low temperature shift furnace 104D2, and the high temperature shift unit includes a high temperature shift furnace 104D1.
The low-temperature shift converter front-end detoxification tank 108DC is internally filled with detoxification agents; the low-temperature shift converter front-end detoxification tank 108DC is arranged in a line between the high-temperature shift unit and the low-temperature shift unit through a pipeline and is used for removing low-temperature shift catalyst poison brought into the low-temperature shift unit by a previous procedure;
the desulfurization unit includes a common desulfurization tank 108DB and a spare desulfurization tank 108DC1 (shown in fig. 2); the installation position of the low-temperature shift converter front-end detoxication tank 108DC is located at the installation position of either the common desulfurization tank 108DB or the spare desulfurization tank 108DC1.
It should be noted that, the low-temperature shift converter front-end detoxification tank 108DC provided in the present application may be a classical fixed bed reactor, and when the classical fixed bed reactor is adopted, one desulfurization tank in the desulfurization unit needs to be removed, and a newly added detoxification tank is installed at the installation position of the removed desulfurization tank. In order to facilitate construction improvement and reduce investment, the low-temperature shift converter front-end detoxification tank 108DC is a standby desulfurization tank 108DC1 of a desulfurization unit for removing desulfurizing agent and separating from other desulfurization tanks. When the standby desulfurization tank 108DC1 is modified, the original desulfurization catalyst in the standby desulfurization tank 108DC1 is removed, and the catalyst is replaced by a detoxication agent (containing a desulfurizing agent and/or a dechlorinating agent) and then is connected to the original low-temperature conversion unit through a pipeline.
In the specific connection mode, as shown in fig. 2, the common desulfurization tank 108DB is connected in parallel with the spare desulfurization tank 108DC1 and then connected in series with the hydrogenation reactor 108DA, and the common desulfurization tank 108DB is separated from the desulfurization unit as the low-temperature shift converter front-end detoxification tank 108DC shown in fig. 1. As shown in fig. 1, the bottom of the low-temperature shift converter front-end detoxification tank 108DC is connected to the top of the low-temperature shift converter 104D2 of the low-temperature shift converter through a pipe to form a series structure, and the top of the low-temperature shift converter front-end detoxification tank 108DC is connected to the lower portion of the high-temperature shift converter 104D1 through a pipe to form a series structure. The bottom of the hydrogenation reactor 108DA is connected to the top of the conventional desulfurization tank 108DB by a pipe to form a series structure.
Because the layout modes of the classical synthetic ammonia production line are basically the same, in order to reduce the distance of laying pipelines as much as possible, the low-temperature shift converter front-end detoxification tank 108DC, the common desulfurization tank 108DB, the hydrogenation reactor 108DA, the low-temperature shift converter 104D2 and the high-temperature shift converter 104D1 are sequentially arranged in a line shape; the bottom and bottom of the standby desulfurization tank 108DB1 in FIG. 2 are connected with the top of the low-temperature shift converter 104D2 through a pipeline to form a series structure, and the low-temperature shift converter is replaced by a front-mounted detoxification tank 108DC as shown in FIG. 1. Of course, in practical application, the additional low-temperature shift converter can be bypassed according to the need so as to change the detoxication agent off-line, specifically, a pipeline is additionally arranged between the top and the bottom of the standby desulfurization tank 108DC1 in FIG. 2 and is connected with the top of the low-temperature shift converter in the low-temperature shift unit to form a series structure.
The feasibility and effect of the scheme provided by the application are verified in an auxiliary manner by analyzing the desulfurization unit and the original low-temperature conversion unit in the classical synthetic ammonia. Raw natural gas in a classical synthesis ammonia production line flows through a primary furnace raw gas preheating coil and then enters a hydrogenation reactor 108DA. A bypass temperature regulating valve is arranged at the feed gas preheating coil, and the temperature of the feed gas entering the hydrogenation reactor 108DA is controlled to be 371 ℃. The bypass temperature regulating valve has high and low alarm, is an air-opening valve and can be operated by a hand wheel. A DCS temperature display table (under EOR conditions) is installed on the pipeline from the preheating coil, and the temperature design value is 396 ℃. The coil and downstream pipeline design parameters were 440 ℃,5,500 kpag.
The heated gas enters a hydrogenation reactor 108DA, and organic sulfur reacts with hydrogen to be converted into H in the reactor filled with the Ni-Mo catalyst 2 S。
H in two zinc oxide desulfurization tanks 108DB and 108DC 2 S and ZnO are removed by reaction, so that the sulfur content in the desulfurized gas is less than 0.1mg/m 3 (volume ratio).
Commonly used desulfurization tank108DB, and the spare desulfurization tank 108DC1 each have inlet and outlet gas distributors. The outlet distributor is a grate plate which acts to prevent catalyst loss and support the process material. Both the common desulfurization tank 108DB and the spare desulfurization tank 108DC1 were 71.8m 3 ZnO type catalyst.
When the Ni-Mo catalyst is filled, the bottom layer of the container is an alumina sphere with the depth of 150mm and the diameter of 25mm, the upper layer is an alumina sphere with the depth of 150mm and the diameter of 13mm, and the upper layer is the Ni-Mo catalyst. A layer of floating screen is installed between the alumina balls and the catalyst to prevent the catalyst from moving. The container also has an inclined discharge channel. A layer of screen mesh is arranged on the catalyst, a layer of 150mm13 mm phi alumina balls are arranged on the screen mesh, and a floating screen mesh and a grate plate are arranged on the alumina balls.
The ZnO catalyst is also filled on alumina balls with the diameter of 25mm, and the alumina balls with the diameter of 13mm, a screen and a grate plate are arranged on the ZnO catalyst as the Ni-Mo catalyst. Each container also has an inclined discharge opening.
Under normal conditions, two desulfurization tanks are operated in series, but the catalyst is prevented from being stopped when the catalyst is replaced, and both desulfurization tanks are in single row or parallel. The pipeline setup allows the order of the two containers to be interchanged. The back of each container inlet stop valve is provided with a filling pipeline, and the pipeline is provided with a double stop valve, a check valve and a drainage shower guide. Is provided with a vent line, and the vent line is provided with a double stop valve and a shower guide. A common outlet pipeline of the two desulfurization tanks also leads out a pipeline to an emptying system, and a manual ball valve is arranged on the pipeline.
The ZnO in each desulfurization tank was replaced approximately every 14 months, with a 14 month replacement calculated by: assuming a normal load of 100% per day through the bed, the sulfur content in the natural gas is 30mg/m 3 The sulfur capacity of the catalyst was 25%. If the sulfur content in the feed gas is small, the catalyst lifetime can be extended. The service life of the Ni-Mo catalyst is about five years, and the catalyst can be recycled. In the classical ammonia synthesis process by hydrocarbon steam reforming, a desulfurization tank is typically provided to remove sulfur compounds from the feed gas. The number of the desulfurization tanks is usually twoAre mutually standby. In actual production, with the improvement of natural gas preparation technology, the sulfur content in the natural gas for synthetic ammonia production is usually low, and the sulfur content of the natural gas is usually less than or equal to 0.7mg/m 3 Far below 30mg/m calculated conditions 3 Therefore, in actual production, a zinc oxide desulfurization tank can be used for many years without replacing an internal ZnO catalyst, and the ZnO catalyst is usually replaced after the ZnO catalyst reaches the service life of the ZnO catalyst, or the ZnO catalyst can be replaced during the maintenance period of the device. Most factories in the prior art are idle for many years due to low sulfur content in raw gas.
According to the analysis, after the ZnO catalyst in the standby desulfurization groove 108DC1 in the desulfurization unit is replaced by the low-temperature conversion catalyst and then is connected into the original low-temperature conversion unit, the normal operation of the desulfurization section of the synthetic ammonia production line is not affected.
The low-temperature shift catalyst arranged in the classical low-temperature shift furnace is usually a dehydrogenation catalyst, and the dehydrogenation catalyst mainly comprises a zinc-based catalyst and a copper-based catalyst, however, the zinc-based catalyst has the defects of overhigh reaction temperature, low selectivity and short service life, so that the industrial application of the zinc-based catalyst is more and more limited. In recent years, researchers at home and abroad have generally shifted the focus to the development of copper-based catalysts, which are mainly copper-based catalysts supported by various oxides or composite oxides, and the performance of the catalysts is modulated by adding various auxiliary agents. The copper catalyst has the advantages of high reaction space velocity, relatively less catalyst consumption, smaller corresponding equipment size and lower reaction temperature when the same amount of alcohol is treated, thereby saving the heat required by the reaction, and prolonging the service life of the catalyst. As is well known to those skilled in the art, the greater the amount of copper-based catalyst used to treat the same amount of process gas, the longer the useful life of the copper-based catalyst. In a classical synthetic ammonia low-temperature catalytic conversion unit, due to the limitation of sites and the like, only two sets of low-temperature conversion furnaces can be arranged, and the size of the low-temperature conversion furnaces is not easy to be oversized, so that the amount of copper-based catalysts in the two sets of low-temperature reactors is limited, the effective service life of the low-temperature conversion unit is usually only 2 to 3 years, and in order to reduce the stop, some manufacturers forcibly prolong the service time of the low-temperature conversion unit, and finally the energy consumption of unit products is increased. Therefore, the service life of the low-temperature conversion unit is prolonged by increasing the amount of the copper-based catalyst for treating the process gas, the synchronous walking with the overhaul period of 2-3 years is achieved, and the catalytic effect of the low-temperature conversion unit can be ensured, so that the method is an effective method.
In the embodiment of the invention, the spare desulfurization tank 108DC1 which is idle as shown in fig. 2 is used as the front-end detoxification tank of the low-temperature conversion furnace, so that the spare desulfurization tank 108DC1 can be used as the front-end detoxification tank 108DC of the low-temperature conversion furnace as shown in fig. 1 while the desulfurization effect is not affected, the poison in the process gas of the previous working procedure is removed, the running period of the device is prolonged, and the production stopping time of the device is shortened.
It will be apparent to those skilled in the art that various modifications and variations can be made to the present invention without departing from the spirit or scope of the invention. Thus, it is intended that the present invention also include such modifications and alterations insofar as they come within the scope of the appended claims or the equivalents thereof.

Claims (5)

1. The low-temperature conversion structure for synthesizing ammonia by a hydrocarbon steam conversion method comprises a desulfurization unit, a hydrogenation reactor, a low-temperature conversion unit and a high-temperature conversion unit, and is characterized by further comprising a front detoxification tank of the low-temperature conversion furnace;
the low-temperature shift converter is internally filled with detoxication agent in a front-mounted detoxication tank; the low-temperature shift converter front-end detoxification tank is arranged in a line between the high-temperature shift unit and the low-temperature shift unit through a pipeline and is used for removing low-temperature shift catalyst poison brought into the low-temperature shift unit by a previous procedure;
the desulfurization unit comprises a common desulfurization tank and a standby desulfurization tank; the installation position of the front detoxification tank of the low-temperature shift converter is positioned at the installation position of any one of the common desulfurization tank or the standby desulfurization tank.
2. The low-temperature shift structure for producing synthetic ammonia by hydrocarbon vapor conversion process according to claim 1, wherein said low-temperature shift converter front-end detoxification tank is said spare desulfurization tank for removing desulfurizing agent and separating from said desulfurization unit.
3. The low temperature shift structure for synthesizing ammonia by hydrocarbon vapor conversion process according to claim 2, wherein the low temperature shift unit comprises a low temperature shift furnace, and the high temperature shift unit comprises a high temperature shift furnace;
the bottom of the front detoxification tank of the low-temperature shift converter is connected with the top of the low-temperature shift converter through a pipeline to form a series structure;
the top of the front detoxification tank of the low-temperature shift converter is connected with the lower part of the high-temperature shift converter through a pipeline to form a series structure;
the bottom of the hydrogenation reactor is connected with the top of the common desulfurization tank through a pipeline to form a series structure.
4. The low-temperature shift structure for synthesizing ammonia by using a hydrocarbon steam reforming process according to claim 3, wherein the low-temperature shift furnace is provided with a detoxification tank, the common desulfurization tank, a hydrogenation reactor, the low-temperature shift furnace and the high-temperature shift furnace which are arranged in a row in sequence.
5. The low temperature shift structure for synthesizing ammonia by steam reforming of hydrocarbons according to claim 1, wherein the detoxicant comprises a desulfurizing agent and/or a dechlorinating agent.
CN202310218281.7A 2023-03-08 2023-03-08 Low-temperature conversion structure for synthesizing ammonia by hydrocarbon steam conversion method Pending CN116239083A (en)

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CN202310218281.7A CN116239083A (en) 2023-03-08 2023-03-08 Low-temperature conversion structure for synthesizing ammonia by hydrocarbon steam conversion method

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CN202310218281.7A CN116239083A (en) 2023-03-08 2023-03-08 Low-temperature conversion structure for synthesizing ammonia by hydrocarbon steam conversion method

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CN116239083A true CN116239083A (en) 2023-06-09

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