Flowable raw material gas catalytic thermal cracking system and process for offshore facilities and vessels

Abstract

A flowable raw material gas catalytic thermal cracking system and process for offshore facilities and vessels. The catalytic thermal cracking system comprises: a reactor (1), communicated with an output end of a sedimentation separator (4) so as to recover a catalyst in the sedimentation separator (4), wherein a conveying tube is arranged in the reactor (1), the end of the conveying tube extending out of the reactor (1) is communicated with a spiral feeding device (3), and the end of the conveying tube introduced to the reactor (1) is opened to receive gas-liquid-solid three-phase materials generated after a catalytic reaction in the reactor (1); a liquid level controller (2), pumping the gas-liquid-solid three-phase materials into the conveying tube; the spiral feeding device (3), configured to convey the gas-liquid-solid three-phase materials into the sedimentation separator (4); the sedimentation separator (4), configured to separate the gas-liquid-solid three-phase materials, wherein the sedimentation separator (4) is provided with a salt feeding port; and a cyclone separation tube (5). The process realizes effective separation of gas-liquid-solid three-phase materials obtained after a reaction, thereby improving the activity of a catalyst, and realizing continuous collection, regeneration and supplementation after the reaction of the catalyst.

Description

Offshore facilities and ship-based mobile raw gas catalytic thermal cracking system and process Technical Field

[0001] The present invention belongs to the technical field of shipbuilding industry equipment systems, and in particular to a flowable raw gas catalytic thermal cracking system and process for use on offshore operating platforms, offshore facilities and ships. Background Art

[0002] Since the Industrial Revolution, the large amount of carbon dioxide emitted by human activities has caused a global warming trend and has increasingly affected human survival. In recent years, major countries around the world have been committed to reducing carbon dioxide emissions.

[0003] Among them, the International Maritime Organization (IMO)'s Fourth Greenhouse Gas Study in 2020 stated that global shipping energy demand in 2018 was close to 11 exajoules (EJ), resulting in about 1 billion tons of carbon dioxide (CO2) being emitted into the atmosphere. This has led to the International Maritime Organization upgrading its emission reduction regulations for the shipping and marine industries. Currently, there are nearly 130 countries that have proposed carbon neutrality goals, of which the vast majority have pledged to achieve carbon neutrality around 2050. Current transitional new energy technologies for ships include methanol, ammonia, etc., while hydrogen energy is considered to be the ultimate fuel solution or post-combustion carbon capture. Hydrogen is considered an ideal energy source for reducing carbon dioxide emissions, and hydrogen fuel cell vehicles, hydrogen burners, hydrogen gas turbines, etc. are being vigorously promoted worldwide. However, traditional fossil fuel hydrogen production plants convert nearly all of the carbon into carbon dioxide during hydrogen production. Therefore, reducing the carbon dioxide produced during hydrogen production using traditional fossil fuels is a global challenge. The current established method involves capturing carbon dioxide from flue gases, but this method is costly, has little economic value, and the captured carbon dioxide is virtually impossible to store stably and economically. Due to these challenges, the high-temperature catalytic thermal cracking of natural gas for hydrogen production was developed many years ago and has been widely recognized by experts and scholars both domestically and internationally. Theoretical research has shown that this process uses approximately 20% less energy than other reaction processes, not only reducing greenhouse gas carbon dioxide emissions but also producing high-value-added solid carbon products.

[0004] However, current research in this field is mostly focused on theoretical research, with weak engineering research and the following main defects: most of them directly fill the molten metal catalyst into the reactor without considering the performance degradation of the catalyst. At the same time, it also does not solve the problem of the catalyst being contaminated by solid carbon products after the reaction, and the problem of the catalyst's reaction activity decreasing after the reaction, which requires the collection, regeneration, and replenishment of the catalyst after the reaction.

[0005] Summary of the Invention

[0006] The present invention aims to provide a mobile feed gas catalytic pyrolysis system and process for offshore facilities and vessels, which achieves effective separation of the gas, liquid, and solid phases after the reaction, thereby improving catalyst activity and enabling continuous collection, regeneration, and replenishment of the catalyst after the reaction. To achieve this objective, the following technical solutions are employed:

[0007] A mobile raw gas catalytic pyrolysis system for offshore facilities and ships, comprising:

[0008] A reactor for carrying out a catalytic reaction, wherein a catalyst is placed therein, wherein a raw gas is introduced into the raw gas inlet end of the reactor; the reactor is connected to the output end of the sedimentation separator to recover the catalyst in the sedimentation separator; a delivery pipe is provided in the reactor, one end of which extends out of the reactor and is connected to the screw feeding device, and the other end of which enters the reactor and is open to receive the gas-liquid-solid three-phase material produced after the catalytic reaction in the reactor;

[0009] A liquid level controller, used for pressurizing the gas-liquid-solid three-phase material into the delivery pipe;

[0010] The spiral feeding device is used to transport the gas-liquid-solid three-phase material into the sedimentation separator;

[0011] The sedimentation separator is used to separate gas, liquid and solid three-phase materials so that the recovered catalyst can flow back into the reactor. Its lower end is connected to the reactor, and its upper end forms a gas outlet for outputting gaseous materials. A salt feeding port is provided on the sedimentation separator. Salt forms a salt layer in the sedimentation separator. The salt layer is used to separate solid and liquid two-phase materials. The separated carbon product is located above the salt layer, and the separated liquid regenerated catalyst is located below the salt layer.

[0012] and a cyclone separation pipe, which is arranged in the sedimentation separator and communicated with the output end of the spiral feeding device, wherein the upper end is communicated with the gas outlet end of the sedimentation separator and the lower end is open and leads into the salt layer.

[0013] Preferably, the liquid level controller is a gravity liquid level controller, comprising a connecting rod and a piston, wherein the connecting rod is arranged outside the reactor and inserted into the reactor, and the piston is located inside the reactor and fixed to the connecting rod, and the connecting rod can move up and down toward the interior of the reactor to pressurize the gas-solid-liquid three-phase material below the conveying pipe into the conveying pipe.

[0014] Preferably, a catalyst feeding port is provided on the sedimentation separator, and the catalyst feeding port is located below the salt layer.

[0015] Preferably, a temperature control system is further provided to maintain the catalyst in a molten state, which is arranged in a section of the sedimentation separator close to the reactor.

[0016] Preferably, the sedimentation separator is provided with a discharge port for discharging solid phase materials and salt layers.

[0017] Preferably, the method further comprises a gas filter connected to the gas outlet end of the sedimentation separator and used for removing solid particles in the gas phase material.

[0018] Preferably, it further comprises a high-temperature heat exchange module, the input end of which is connected to the output end of the gas filter for heat recovery.

[0019] Preferably, a gas distribution element is provided at the raw gas input end of the reactor.

[0020] A process for catalytic thermal cracking of mobile raw gas for offshore facilities and ships, comprising the following steps:

[0021] Step 1: Add catalyst into the reactor from the catalyst feed port; the preheated raw gas is introduced into the reactor through the distributor element to start the catalytic cracking reaction; the gas-solid-liquid three-phase is generated in the reactor;

[0022] Step 2: Start the liquid level controller and the screw feeding device. The liquid level controller pushes the gas-liquid-solid three-phase material into the screw feeding device. The gas-liquid-solid three-phase material enters the cyclone separation tube through the screw feeding device.

[0023] Step 3: The gas-liquid-solid three-phase material is in a swirling state in the cyclone separation tube. The gas-liquid-solid three-phase material enters the upper part of the cyclone separation tube upward. As the diameter of the cyclone separation tube is expanded, the flow rate of the solid and liquid phase materials is reduced, and the gas phase material is separated from the solid and liquid phase materials; the gas phase material passes through the top of the cyclone separation tube and enters the gas filter for filtration;

[0024] The solid and liquid phase materials flow downward into the lower part of the cyclone separation tube due to gravity, and finally enter the salt layer of the sedimentation separator through the lower end of the cyclone separation tube;

[0025] Step 4: Separating the solid phase material from the liquid phase material in the salt layer to obtain a solid carbon product;

[0026] Step 5: The liquid phase material flows back to the sedimentation separator after passing through the salt layer to achieve continuous regeneration of the catalyst.

[0027] Compared with the prior art, the advantages of the present invention are:

[0028] (1) The problem of catalyst contamination caused by solid carbon products and the decrease in the reaction activity of the catalyst after the reaction, which requires continuous collection, regeneration, and replenishment of the catalyst after the reaction, is solved. Specifically: the liquid level controller, screw feeding device, and sedimentation separation system (seditioner + cyclone separation tube) realize the continuous and effective separation of the gas, liquid, and solid phases after the reaction, thereby improving the catalyst activity, realizing the removal and replenishment of the catalyst after the reaction, improving the activity of the overall catalytic reaction, increasing the system's ability to operate for a long time, and improving the conversion rate of catalytic cracking, improving the efficiency of carbon capture in the overall process, and making industrialization possible.

[0029] (2) Considering the performance degradation of the catalyst, a salt feeding port is set to replenish the catalyst. The catalyst feeding port is located below the salt layer, and the fresh catalyst feeding port is in the lower part of the sedimentation separator. This part can be adjusted according to the changes in the reaction to maintain the activity of the catalyst.

[0030] (3) The invention has a wide range of applications: in application scenarios such as offshore facilities and ships, this technology will be used to achieve zero-carbon / low-carbon energy supply.

[0031] (4) The application of this invention can significantly reduce greenhouse gas emissions, optimize the overall energy conservation and emission reduction performance of the marine industry, and help achieve the "dual carbon" goal. BRIEF DESCRIPTION OF THE DRAWINGS

[0032] FIG1 is a structural diagram of an offshore facility and a ship-mounted flowable raw gas catalytic thermal cracking system.

[0033] Among them, 1-reactor, 11-gas distribution element, 2-liquid level controller, 21-piston, 3-screw feeding device, 4-sedimentation separator, 41-discharge port, 42-catalyst discharge port, 5-cyclone separation tube, 6-gas filter, 7-high-temperature heat exchange module, 8-flow control system. DETAILED DESCRIPTION

[0034] The following is a more detailed description of the offshore facility and the ship-mounted mobile feed gas catalytic pyrolysis system and process of the present invention, with reference to schematic diagrams. Preferred embodiments of the present invention are shown, and it should be understood that those skilled in the art may modify the invention described herein while still achieving the advantageous effects of the present invention. Therefore, the following description should be understood as generally known to those skilled in the art and is not intended to limit the present invention.

[0035] As shown in FIG1 , the mobile raw gas catalytic pyrolysis system for offshore facilities and ships includes: a reactor 1 , a gravity liquid level controller, a screw feeding device 3 , a sedimentation separator 4 and a cyclone separation tube 5 .

[0036] Feed gases include, but are not limited to, natural gas, methane, H2S, NH3, and organic hydrocarbon gases. After heat exchange in a high-temperature heat exchange module (which recovers heat from the desorbed gas after catalytic cracking), the feed gases are preheated and then enter reactor 1, where they come into contact with the molten metal catalyst, undergoing a catalytic cracking reaction to produce hydrogen and solid carbon products. In this embodiment, natural gas is used as the reaction gas to illustrate the system.

[0037] Reactor 1 is used for catalytic reaction, is vertically arranged and has a catalyst placed therein. Raw gas is introduced into the raw gas inlet end of reactor 1, and a gas distribution element 11 is provided at the raw gas input end of reactor 1; reactor 1 is connected to the output end of sedimentation separator 4 to recover the purified catalyst in sedimentation separator 4.

[0038] At the lower part of the sedimentation separator 4, the other end below the catalyst feeding port is a catalyst discharge port 42, which is used for stopping the operation and emptying the catalyst.

[0039] A delivery pipe is provided in the reactor 1 , one end of which extends out of the reactor 1 and is connected to the screw feeding device 3 ; the end thereof which enters the reactor 1 is open to receive the gas-liquid-solid three-phase material produced after the catalytic reaction in the reactor 1 .

[0040] In this embodiment, a tubular reactor 1 is used, including but not limited to bubbling beds, stirred beds, fluidized beds, fixed beds, and suspended beds. Gas distribution elements 11 include but are not limited to gas bricks, gas distribution plates, and gas distributors; the selected materials must be corrosion-resistant, high-temperature-resistant, and high-pressure-resistant.

[0041] After the organic hydrocarbon reaction gas undergoes catalytic reaction, hydrogen and solid carbon products are produced. As the reaction continues, the solid carbon product is not completely separated from the catalyst, and some carbon products will accumulate in the catalyst, reducing the activity of the catalyst. The existing technology does not reflect an effective solution to this problem. To solve this problem, this process sets a "gravity liquid level controller" on the upper part of the reactor 1. According to the reaction process, when the conversion rate has a downward trend and the catalyst performance needs to be optimized, the gravity liquid level controller (connecting rod) is started by an external driving component (such as a hydraulic cylinder). The reciprocating piston 21 is controlled by the connecting rod to penetrate into the interior of the reactor 1, pushing the liquid catalyst, carbon products, and analytical gas (including hydrogen generated after cracking and raw gas that has not been completely cracked) into the spiral feeding device 3, and finally into the cyclone separation tube 5.

[0042] Specifically, the liquid level controller 2 pressurizes the gas-liquid-solid three-phase material (liquid catalyst, carbon product, and desorbed gas) into the delivery pipe. In this embodiment, the liquid level controller 2 is a gravity level controller comprising a connecting rod and a piston 21. The connecting rod is disposed outside the reactor 1 and inserted into the reactor 1. The piston 21 is located inside the reactor 1 and is fixed to the connecting rod. The connecting rod can move up and down in the interior of the reactor 1 to pressurize the gas-solid-liquid three-phase material below the delivery pipe into the delivery pipe.

[0043] The material of the gravity liquid level controller is preferably 617, 310S, HR120, titanium alloy, etc. (the manufacturer can provide the corresponding material). The gravity liquid level controller regulates the activity space inside the reactor 1 to achieve control and flow of the catalyst liquid level, avoid the occurrence of back mixing, and ensure that the catalyst and solid carbon enter the cyclone separation tube 5 safely and efficiently.

[0044] Due to temperature changes, the molten catalyst is prone to flow pattern changes during transportation and may even clog the pipeline. Therefore, a screw feeding device 3 is designed.

[0045] The screw feeding device 3 is used to convey the gas-liquid-solid three-phase material into the sedimentation separator 4. The screw feeding device 3 adopts shaft-coupled screw conveying, electric drive, and must be explosion-proof, with a grade of not less than CT4. The main body structure is a spiral structure, and the screw conveyor is inclined, with a preferred inclination angle of 10-20°. The principle of the screw conveyor is that the rotating spiral blades push the gas-liquid-solid three-phase material to be conveyed by the screw conveyor. The force that prevents the material from rotating with the screw conveyor blades is the material's own weight and the friction resistance of the spiral conveying pipe to the material. The spiral blades welded on the rotating shaft of the screw conveyor have different surface shapes, such as solid surface type, belt surface type, and blade surface type, depending on the conveyed material. The blades, including all parts that come into contact with the gas-solid-liquid three-phase, are preferably made of high-temperature and corrosion-resistant alloy steel (models 617, 310S, HR120, titanium alloy, etc.). In the natural gas catalytic cracking process, the use of a molten catalyst is a catalytic cracking method with a relatively high conversion rate. However, when the molten catalyst is subjected to a high temperature of 1000°C, low-melting-point metals such as bismuth and tin may escape in the form of metal vapor, causing damage to the pipeline, the interior of the reactor 1, and high-temperature resistant metal parts. After the reaction, the catalyst contains a large amount of solid carbon, which reduces the catalyst's reactivity and can clog the pipeline. Current technologies are unable to effectively address this issue.

[0046] In this embodiment, the sedimentation separator 4 is a liquid-solid separation device used to separate the liquid catalyst from the solid carbon after the reaction. This device and the cyclone separation tube 5 share the same cavity. The evaporated salt gas does not block the outlet pipe, but adheres to the inner wall of the sedimentation separator 4 and regenerates into a solid salt product.

[0047] Specifically, the sedimentation separator 4 is used to separate the gas-liquid-solid three-phase materials. It is tilted to allow the recovered catalyst to flow back into the reactor 1. Its lower end is connected to the reactor 1, and its upper end forms a gas outlet for discharging the gaseous material. The sedimentation separator 4 has a salt feed port. The salt forms a salt layer inside the sedimentation separator 4, which is used to separate the solid-liquid two-phase materials. The solid-liquid two-phase materials mainly consist of molten catalyst and solid carbon product.

[0048] The salt feed port is located above the sedimentation separator 4. When the molten catalyst and desorption gas (including hydrogen generated after cracking and uncompleted raw gas) pass through the screw feeder 3 and enter the cyclone separation tube 5, salt addition begins. When the screw feeder 3 is activated, the "salt addition" chain is activated. Salt addition is pneumatic, and the amount of salt added is time-controlled.

[0049] The settling separator 4 is tilted, preferably at an angle of 30 to 60 degrees, to facilitate the settling and reflow of the catalyst after passing through the salt layer. A temperature control system is located at the bottom of the settling separator 4, maintaining a higher temperature there and decreasing the temperature inside the settling separator 4 from bottom to top, thereby maintaining the metal catalyst in a molten state and settling at the bottom of the settling separator. The tilt design is intended to utilize density differences (the density of the catalyst is greater than that of the salt, which is greater than that of solid carbon) to facilitate stratified recovery of the material. The molten metal catalyst decarbonized by the settling separator 4 is returned to the reactor 1 through the flow control system 8 for recycling. Specifically, the flow control system 8 takes into account the density of the molten metal catalyst and, at the bottom of the settling separator 4, incorporates a buffer baffle and a flow control valve to prevent damage to the pipeline and equipment due to differences in the flow state of the molten metal catalyst. Through experiments and simulations, the valve opening and residence time can be accurately calculated, thereby ensuring that the molten metal catalyst can return to the reactor 1 without bringing salt and carbon back into the reactor 1.

[0050] The middle part of the upper and lower interfaces (lower interface - interface with reactor 1, upper interface - interface with gas filter 6) of the sedimentation separator 4 is a material layer that can effectively separate the catalyst and solid carbon product, that is, a salt layer, mostly inorganic salts, and the selected materials include but are not limited to: NaCl, NaBr, MnCl2, KCl, etc.

[0051] A catalyst feeding port for replenishing catalyst is set on the sedimentation separator 4. The catalyst feeding port is located below the salt layer. The fresh catalyst feeding port is in the lower middle part of the sedimentation separator 4. The position of this part can be adjusted according to the changes in the reaction. It is an important part to maintain the activity of the catalyst.

[0052] The sedimentation separator 4 is also provided with a discharge port 41 for discharging solid phase materials and salt layers. The separated salt and carbon are accumulated in the sedimentation separator 4, and the carbon product can be continuously removed. After the reaction cycle is completed and the system is shut down, the salt and carbon product and other solid materials are discharged.

[0053] The reaction chamber of the sedimentation separator 4 is sealed, which can effectively reduce the volatile materials under high temperature conditions, for example, salt evaporation enters the upstream and downstream pipelines, forms crystals, and causes blockage.

[0054] The principles for separating solid-liquid materials in a salt layer are as follows: 1) Because the density of solid carbon is less than that of the salt layer, which is also less than that of the catalyst, and the density of the catalyst is greater than that of the salt layer, gravity separates the three phases. 2) Because the polarity of the catalyst is greater than that of the salt, which in turn is greater than that of the solid carbon, the salt becomes an effective medium for separating the catalyst from the carbon when the three phases are mixed. Based on either of these principles, solid-liquid separation in a salt layer can be achieved.

[0055] The temperature control system is used to maintain the catalyst in a molten state and is located at one end of the sedimentation separator 4 near the reactor 1. The present invention designs the sedimentation reaction to add salt from the top. The temperature of the lower part of the sedimentation separator 4 is to maintain the molten state of the metal catalyst. Therefore, when the temperature of the salt layer decreases from bottom to top, the salt layer in direct contact with the catalyst will more easily become molten, naturally forming a physical barrier, which can effectively prevent the metal vapor from escaping upward and increase the stability of the catalyst.

[0056] Cyclone separation tube 5 is disposed within sedimentation separator 4 and communicates with the output end of screw feeder 3. Its upper end is connected to the gas outlet of sedimentation separator 4, while its lower end is open and extends into the salt layer, allowing the molten catalyst and solid carbon within it to enter the salt layer. Specifically, the lower portion of cyclone separation tube 5 extends into the middle two-thirds of the salt layer of sedimentation separator 4.

[0057] Specifically, the cyclone 5 achieves gas-solid-liquid separation, employing a larger-at-top, smaller-at-bottom structure. Preferably, the material delivery pipe is tangentially connected to the cyclone 5, causing the material to swirl within the tube, facilitating the separation of the gaseous phase from the liquid and solid phases. Once the material enters the cyclone 5, the liquid and solid phases flow downward from the separation tube into the sedimentation separator 4.

[0058] Specifically, the gaseous material flows upward into the upper portion of the cyclone 5. Due to the sudden expansion of the tube diameter, the flow rate decreases, and the gas and solid phases naturally separate. The gaseous material passes through the top of the cyclone 5, is filtered, and then compressed and enters the PSA device for gas purification. Due to gravity, the solid and liquid phases flow downward into the lower portion of the cyclone 5 and ultimately enter the sedimentation separator 4.

[0059] As for the metal vapor that may escape during the reaction process, due to the sudden expansion of the pipe diameter, the flow rate is reduced and the temperature at this location is low, the metal vapor can be condensed and refluxed into the sedimentation separator 4.

[0060] Gas filter 6 is connected to the outlet of sedimentation separator 4 and is used to remove solid particles from the gaseous material. Specifically, the high-temperature desorbed gas (containing hydrogen and unreacted raw gas) passes through gas filter 6, where a small amount of solid particles are removed from the gas phase. It then flows into high-temperature heat exchange module 7, where it exchanges heat with the unreacted raw gas for heat recovery. After cooling at the terminal, this gas enters the PSA pressure swing adsorption (PSA) process to purify the hydrogen.

[0061] Offshore facilities and ship-based mobile raw gas catalytic thermal cracking process, specifically:

[0062] Step 1: Add catalyst from the catalyst feed port and pass it into the reactor 1 through the flow control system 8. The preheated feed gas is passed into the reactor 1 through the distributor element 11 to start the catalytic cracking reaction. The gas, solid and liquid three phases are generated in the reactor 1.

[0063] Step 2: Start the liquid level controller 2 and the screw feeding device 3. The liquid level controller 2 pushes the gas-liquid-solid three-phase material into the screw feeding device 3. The gas-liquid-solid three-phase material enters the cyclone separation tube 5 through the screw feeding device 3.

[0064] Step 3: The gas-liquid-solid three-phase material is in a cyclonic state in the cyclone separation tube 5. The gas-liquid-solid three-phase material enters the upper part of the cyclone separation tube 5 upward. As the diameter of the cyclone separation tube 5 is expanded, the flow rate of the solid and liquid phase materials is reduced, and the gas phase material is separated from the solid and liquid phase materials.

[0065] The gaseous material passes through the top of the cyclone separation tube 5 and enters the gas filter 6 for filtration.

[0066] The solid and liquid phase materials flow downward into the lower part of the cyclone separation tube 5 due to gravity, and finally enter the salt layer of the sedimentation separator 4 through the lower end of the cyclone separation tube 5.

[0067] Step 4: Separate the solid phase material and the liquid phase material in the salt layer.

[0068] Step 5: The liquid phase material flows back to the lower part of the sedimentation separator 4 after passing through the salt layer.

[0069] The above description is merely a preferred embodiment of the present invention and does not limit the present invention in any way. Any person skilled in the art who, without departing from the scope of the present invention, makes any equivalent substitution, modification, or other changes to the technical solution and technical content disclosed in the present invention shall be deemed to be within the scope of the present invention and still fall within the scope of protection of the present invention.

Claims

1. A mobile raw gas catalytic thermal cracking system for offshore facilities and ships, characterized in that: include: A reactor, used for catalytic reaction, wherein a catalyst is placed, and a raw material gas is introduced into the raw material gas inlet end of the reactor; The reactor is connected to the output end of the sedimentation separator to recover the catalyst in the sedimentation separator; A delivery pipe is arranged in the reactor, one end of which extends out of the reactor and is connected to the screw feeding device, and one end of which enters the reactor and is open to receive the gas-liquid-solid three-phase material produced after the catalytic reaction in the reactor; A liquid level controller, used for pressurizing gas-liquid-solid three-phase materials into the delivery pipe; The spiral feeding device is used to transport the gas-liquid-solid three-phase material into the sedimentation separator; The sedimentation separator is used to separate gas-liquid-solid three-phase materials so that the recovered catalyst can flow back into the reactor. Its lower end is connected to the reactor, and its upper end forms a gas outlet for outputting gas-phase materials. The sedimentation separator is provided with a salt feeding port and a catalyst feeding port. Salt forms a salt layer in the sedimentation separator. The salt layer is used for separation of solid-liquid two-phase materials. The separated carbon product is located above the salt layer, and the separated liquid regenerated catalyst is located below the salt layer. The catalyst feeding port is located below the salt layer. and a cyclone separation pipe, which is arranged in the sedimentation separator and communicated with the output end of the spiral feeding device, the upper end of which is communicated with the gas outlet end of the sedimentation separator, and the lower end is open and leads into the salt layer; A temperature control system is further provided to keep the catalyst in a molten state, and is disposed at one end of the sedimentation separator close to the reactor.

2. The offshore facility and ship-based mobile raw gas catalytic thermal cracking system according to claim 1, characterized in that: The sedimentation separator is provided with a discharge port for discharging part of the carbon product and the salt layer.

3. The offshore facility and ship-based mobile raw gas catalytic thermal cracking system according to claim 1, characterized in that: The device further comprises a gas filter which is communicated with the gas outlet end of the sedimentation separator and is used for removing solid particles in the gas phase material.

4. The offshore facility and ship-based mobile raw gas catalytic thermal cracking system according to claim 3, characterized in that: It further comprises a high-temperature heat exchange module, the input end of which is connected to the output end of the gas filter for heat recovery.

5. The offshore facility and ship-based mobile raw gas catalytic thermal cracking system according to claim 1, characterized in that: A gas distribution element is arranged at the raw gas input end of the reactor.

6. A flowable raw gas catalytic thermal cracking process using the offshore facility and the ship-based flowable raw gas catalytic thermal cracking system according to any one of claims 1 to 5, characterized in that: The following steps are involved: Step 1, adding catalyst into the reactor from the catalyst feed port; the preheated raw gas is introduced into the reactor through the distributor element to start catalytic thermal cracking reaction; gas-solid-liquid three-phase is generated in the reactor; Step 2: Start the liquid level controller and the screw feeding device. The liquid level controller pushes the gas-liquid-solid three-phase material into the screw feeding device. The gas-liquid-solid three-phase materials enter the cyclone separation tube through the spiral feeding device; Step 3: The gas-liquid-solid three-phase material is in a cyclone state in the cyclone separation tube, and the gas-liquid-solid three-phase material enters the upper part of the cyclone separation tube upward. As the diameter of the cyclone separation tube is enlarged, the flow rate of the solid and liquid phase materials is reduced, and the gas phase material is separated from the solid and liquid phase materials; the gas phase material enters the gas filter through the top of the cyclone separation tube for filtration; Due to the action of gravity, the solid and liquid phase materials flow downward into the lower part of the cyclone separation tube, and finally enter the salt layer of the sedimentation separator through the lower end of the cyclone separation tube; Step 4: Separating the solid phase material from the liquid phase material in the salt layer to obtain a solid carbon product; Step 5: The liquid phase material flows back to the sedimentation separator after passing through the salt layer to realize the continuous regeneration of the catalyst.

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