CN116712947B - Offshore facility and marine flowable raw material gas catalytic pyrolysis system and process - Google Patents
Offshore facility and marine flowable raw material gas catalytic pyrolysis system and process Download PDFInfo
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Classifications
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- 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
- Y02P20/584—Recycling of catalysts
Abstract
The invention provides a catalytic pyrolysis system and a catalytic pyrolysis process for offshore facilities and marine flowable raw material gas, wherein the catalytic pyrolysis system comprises: the reactor is communicated with the output end of the sedimentation separator to recycle the catalyst in the sedimentation separator; a conveying pipe is arranged in the reactor, one end of the conveying pipe, which extends out of the reactor, is communicated with the spiral feeding device, and one end of the conveying pipe, which is introduced into the reactor, is opened to receive gas-liquid-solid three-phase materials generated after catalytic reaction in the reactor; the liquid level controller is used for conveying the gas-liquid-solid three-phase materials into the conveying pipe in a pressing way; the spiral feeding device is used for conveying the gas-liquid-solid three-phase materials into the sedimentation separator; the sedimentation separator is used for separating gas-liquid-solid three-phase materials; the sedimentation separator is provided with a salt feeding port and a cyclone separation pipe. The invention realizes the effective separation of the gas, liquid and solid phases after the reaction, thereby improving the activity of the catalyst and realizing the continuous collection, regeneration and supplementation of the catalyst after the reaction.
Description
Technical Field
The invention belongs to the technical field of ship industrial equipment systems, and particularly relates to a catalytic pyrolysis system and a catalytic pyrolysis process for a flowable raw material gas applied to offshore facilities and ships.
Background
Since the industrial revolution, carbon dioxide emitted in large amounts by human activities has tended to warm the world and has increasingly affected the survival of humans themselves.
The fourth greenhouse gas research report in International Maritime Organization (IMO) 2020 states that global shipping energy requirements in 2018 are approaching 11 kilojoules (EJ), resulting in the release of about 10 hundred million tons of carbon dioxide (CO 2) into the atmosphere. This has led to the upgrade of emission reduction regulations in the marine and marine industries by the international maritime organization. Current transitional marine new energy technologies include methanol, ammonia, etc., while hydrogen energy is considered the ultimate fuel solution or post-combustion carbon capture. Hydrogen is considered as an ideal energy source for reducing carbon dioxide emissions, and hydrogen fuel cell automobiles, hydrogen combustors, hydrogen gas turbines, and the like are being widely popularized worldwide. However, the traditional fossil fuel hydrogen production device is used for preparing hydrogen, and almost all carbon elements are converted into carbon dioxide, so that the problem of reducing the carbon dioxide generated during hydrogen production when the traditional fossil fuel hydrogen production device is adopted is a current world problem, the current mature method is used for capturing carbon dioxide in flue gas, but the method is high in cost and almost has no economic value, and the captured carbon dioxide can not be stored economically and stably; based on the problems, the high-temperature catalytic thermal cracking hydrogen production mechanism of natural gas has been accepted by most domestic and foreign expert students for many years. Theoretical research shows that the natural gas high-temperature catalytic thermal cracking hydrogen production process saves about 20% of energy consumption compared with other reaction processes, reduces the emission of greenhouse gas carbon dioxide, and can also produce solid carbon products with high added value.
However, most of the research in the field is focused on theoretical research, engineering research is weak, and the following defects mainly exist: most of the metal catalysts in the molten state are directly filled in the reactor, the performance attenuation of the catalysts is not considered, and the problems that the catalysts after the reaction are polluted by solid carbon products, the reactivity of the catalysts after the reaction is reduced and the catalysts need to be collected, regenerated and replenished after the reaction are not solved.
Disclosure of Invention
The invention aims to provide a catalytic pyrolysis system and a catalytic pyrolysis process for offshore facilities and marine flowable raw material gas, which realize the effective separation of gas, liquid and solid phases after reaction, thereby improving the activity of a catalyst and realizing the continuous collection, regeneration and supplementation of the catalyst after reaction. In order to achieve the above purpose, the following technical scheme is adopted:
an offshore facility and marine flowable feed gas catalytic thermal cracking system comprising:
the reactor is used for carrying out catalytic reaction, a catalyst is placed in the reactor, and the raw material gas inlet end of the reactor is filled with raw material gas; the reactor is communicated with the output end of the sedimentation separator to recycle the catalyst in the sedimentation separator; the reactor is internally provided with a conveying pipe, one end of the conveying pipe, which extends out of the reactor, is communicated with the spiral feeding device, and one end of the conveying pipe, which is introduced into the reactor, is opened to receive gas-liquid-solid three-phase materials generated after catalytic reaction in the reactor;
the liquid level controller is used for conveying the gas-liquid-solid three-phase materials into the conveying pipe in a pressing mode;
the spiral feeding device is used for conveying the gas-liquid-solid three-phase materials into the sedimentation separator;
the sedimentation separator is used for separating gas-liquid-solid three-phase materials so that the recovered catalyst flows back into the reactor, the lower end of the sedimentation separator is communicated with the reactor, and the upper end of the sedimentation separator forms an air outlet end for outputting gas-phase materials; a salt charging port is formed in the sedimentation separator; salt forms a salt layer in the sedimentation separator; the salt layer is used for separating 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.
And the cyclone separation pipe is arranged in the sedimentation separator and is communicated with the output end of the spiral feeding device, the upper end of the cyclone separation pipe is communicated with the air outlet end of the sedimentation separator, and the lower end of the cyclone separation pipe is opened and is led into the salt layer.
Preferably, the liquid level controller is a gravity liquid level controller and comprises a connecting rod and a piston, wherein the connecting rod is arranged outside the reactor and inserted into the reactor, the piston is positioned in the reactor and fixed on the connecting rod, and the connecting rod can move up and down towards the inside of the reactor so as to press and send the gas-solid-liquid three-phase materials below the conveying pipe into the conveying pipe.
Preferably, a catalyst feed inlet is arranged on the sedimentation separator, and the catalyst feed inlet is positioned below the salt layer.
Preferably, a temperature control system is further provided to maintain the catalyst in a molten state, which is provided at a section of the sedimentation separator near the reactor.
Preferably, a discharging port for discharging the solid-phase materials and the salt layer is arranged on the sedimentation separator.
Preferably, the gas filter is in communication with the outlet end of the sedimentation separator and is used for removing solid particles in the gas phase material.
Preferably, the high-temperature heat exchange module further comprises an input end which is communicated with the output end of the gas filter for heat recovery.
Preferably, the raw material gas input end of the reactor is provided with a gas distribution element.
An offshore facility and marine flowable feed gas catalytic thermal cracking process comprising the steps of:
step 1, adding a catalyst into a reactor from a catalyst feed port; the preheated raw material gas is introduced into the reactor through the distributor element to start catalytic cracking reaction; generating gas-solid-liquid three phases in the reactor;
step 2, starting a liquid level controller and a spiral feeding device, wherein the liquid level controller pushes the gas-liquid-solid three-phase material to enter the spiral feeding device; the gas-liquid-solid three-phase material enters a cyclone separation pipe through a spiral feeding device;
step 3, the gas-liquid-solid three-phase materials are in a cyclone state in the cyclone separation pipe, the gas-liquid-solid three-phase materials enter the upper part of the cyclone separation pipe upwards, and as the pipe diameter of the cyclone separation pipe is enlarged, the flow speed of the solid-liquid phase materials is reduced, and the gas-phase materials are separated from the solid-liquid phase materials;
the gas phase material enters a gas filter for filtration through the top of a cyclone separation pipe;
the solid-liquid phase material enters the lower part of the cyclone separation pipe downwards under the action of gravity and finally enters the salt layer of the sedimentation separator through the lower end of the cyclone separation pipe;
step 4, separating the solid phase material and the liquid phase material in a salt layer to obtain a solid carbon product;
and 5, refluxing the liquid phase material to a sedimentation separator after passing through a salt layer, and realizing continuous regeneration of the catalyst.
Compared with the prior art, the invention has the advantages that:
(1) Solves the problems that the catalyst after reaction causes pollution to the catalyst due to solid carbon products, the reactivity of the catalyst after reaction is reduced, and continuous collection, regeneration and supplementation are required after the catalyst is reacted. Specific: the liquid level controller, the spiral feeding device and the sedimentation separation system (sedimentation separator and cyclone separation pipe) realize continuous and effective separation of gas, liquid and solid phases after reaction, so that the activity of the catalyst is improved, impurity removal and supplementation after the catalyst reaction are realized, the activity of the whole catalytic reaction is improved, the capability of the system for long-time operation is improved, the conversion rate of catalytic cracking is improved, the efficiency of capturing carbon in the whole process is improved, and industrialization is possible.
(2) Considering the performance attenuation of the catalyst, a salt feed port is arranged for supplementing the catalyst, the catalyst feed port is positioned below a salt layer, and a fresh catalyst feed port is positioned at the middle lower part of the sedimentation separator, and the position of the fresh catalyst feed port can be adjusted according to the changing condition of the reaction, so that the activity of the catalyst is maintained.
(3) The invention has wide application range: in offshore facilities and vessels etc. application scenarios, the technology will be used to achieve zero carbon/low carbon energy supply.
(4) After the invention is applied, the emission of greenhouse gases can be greatly reduced, and the integral energy-saving and emission-reducing performance of the marine industry is optimized.
Drawings
FIG. 1 is a block diagram of a catalytic pyrolysis system for offshore facilities and a marine flowable feed gas.
The device comprises a 1-reactor, a 11-gas distribution element, a 2-liquid level controller, a 21-piston, a 3-spiral feeding device, a 4-sedimentation separator, a 41-discharge port, a 42-catalyst discharge port, a 5-cyclone separation tube, a 6-gas filter, a 7-high temperature heat exchange module and an 8-flow control system.
Detailed Description
The offshore facility and marine flowable feed gas catalytic thermal cracking system and process of the present invention will be described in more detail below with reference to the schematic drawings, in which preferred embodiments of the present invention are shown, it being understood that one skilled in the art may modify the invention described herein while still achieving the advantageous effects of the invention. Accordingly, the following description is to be construed as broadly known to those skilled in the art and not as limiting the invention.
As shown in fig. 1, the catalytic pyrolysis system for offshore facilities and marine flowable feed gas comprises: a reactor 1, a gravity liquid level controller, a spiral feeding device 3, a sedimentation separator 4 and a cyclone separation pipe 5.
Raw material gases, including but not limited to: natural gas, methane, H 2 S、NH 3 Organic hydrocarbon gas. The raw material gas is preheated after heat exchange by a high-temperature heat exchange module (the high-temperature heat exchange module recovers the heat of the analysis gas after catalytic pyrolysis), enters a reactor 1, fully contacts with a molten metal catalyst, and undergoes catalytic cracking reaction to generate hydrogen and a solid carbon product. In this embodiment, the reaction gas is exemplified by natural gas, and the system will be described.
The reactor 1 is used for carrying out catalytic reaction, is vertically arranged and is internally provided with a catalyst, the raw material gas inlet end of the reactor 1 is filled with raw material gas, and the raw material gas input end of the reactor 1 is provided with a gas distribution element 11; the reactor 1 communicates with the output of the sedimentation separator 4 to recover the purified catalyst in the sedimentation separator 4.
The lower part of the sedimentation separator 4, the other end below the catalyst feed inlet is a catalyst discharge outlet 42 for stopping and emptying the catalyst.
A conveying pipe is arranged in the reactor 1, and one end of the conveying pipe extending out of the reactor 1 is communicated with the spiral feeding device 3; one end of the catalyst is opened to receive gas-liquid-solid three-phase materials generated after catalytic reaction in the reactor 1.
In the present embodiment, the tubular reactor 1 is employed, including but not limited to: bubbling bed, stirred bed, fluidized bed, fixed bed, suspended bed, etc. The gas distribution member 11 includes, but is not limited to: air brick, air distribution plate and air distributor; the selected material should be corrosion resistant, high temperature resistant and high pressure resistant.
After the organic hydrocarbon reaction gas is subjected to catalytic reaction, hydrogen and solid carbon products are generated, and as the reaction is continued, the solid carbon products are not thoroughly separated from the catalyst, and part of the carbon products are accumulated in the catalyst to reduce the activity of the catalyst, so that an effective scheme for solving the problem is not presented in the prior art. In order to solve the problem, the process is provided with a gravity liquid level controller at the upper part of the reactor 1, when the conversion rate has a decreasing trend according to the reaction process and the catalyst needs to be subjected to performance optimization, an external driving component (such as a hydraulic cylinder) is used for starting the gravity liquid level controller (a connecting rod), a reciprocating piston 21 is controlled through the connecting rod, the reciprocating piston is extended into the reactor 1, and liquid catalyst, carbon products and analysis gas (including hydrogen generated after cracking and raw gas which does not completely react after cracking) are pushed into the spiral feeding device 3 and finally introduced into the cyclone separation tube 5.
Specifically, the liquid level controller 2 is used for conveying the gas-liquid-solid three-phase materials (liquid catalyst, carbon product and analysis gas) into the conveying pipe under pressure. In this embodiment, the liquid level controller 2 is a gravity liquid level controller, and includes 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 disposed in the reactor 1 and fixed to the connecting rod, and the connecting rod can move up and down towards the inside of the reactor 1, so as to press and send the gas-solid-liquid three-phase material under the conveying pipe into the conveying pipe.
The gravity liquid level controller is preferably 617 materials, 310S, HR120, titanium alloy and the like (manufacturers can provide corresponding materials), and regulates and controls the movable space inside the reactor 1, so that the control and flow of the catalyst liquid level are realized, the occurrence of back mixing is avoided, and the safe and efficient entering of the catalyst and the solid carbon into the cyclone separation tube 5 is ensured.
The spiral feeding device 3 is designed because the flow pattern of the molten catalyst is changed or even the pipeline is blocked in the conveying process due to the change of the temperature.
And the spiral feeding device 3 is used for conveying the gas-liquid-solid three-phase materials into the sedimentation separator 4. The spiral feeding device 3 adopts shaft-linked spiral conveying, is electrically driven, is explosion-proof and has the grade not less than CT4. The body structure is a spiral structure, the spiral conveyor is obliquely arranged, and the preferred inclination angle is 10-20 degrees. The principle of the screw conveyor is that the rotating screw blade pushes the gas-liquid-solid three-phase material to convey the material by the screw conveyor, so that the force for preventing the material from rotating together with the screw conveyor blade is the self weight of the material and the friction resistance of the screw conveying pipeline to the material. The surface type of the spiral blade welded on the rotating shaft of the spiral conveyor has solid surface type, belt surface type, blade surface type and other types according to the different conveying materials. The blade comprises all the materials contacting with the gas, solid and liquid three-phase parts, and is preferably made of high-temperature and corrosion resistant alloy steel (types 617, 310S, HR120, titanium alloy and the like)
In the catalytic cracking process of natural gas, a molten catalyst is used as a catalytic cracking mode with higher conversion rate, but the molten catalyst is at high temperature of 1000 ℃, wherein metals with low melting points, such as bismuth, tin and the like, possibly escape in the form of metal vapor, and damage to pipelines and the inside of the reactor 1 and high-temperature-resistant metal parts can be caused; the catalyst contains a large amount of solid carbon after the reaction, so that the reactivity of the catalyst can be reduced, the solid carbon can block a pipeline, and the prior art cannot effectively treat the solid carbon.
In this embodiment, the sedimentation separator 4 is a device for implementing liquid-solid separation, and is used for separating the reacted liquid catalyst from the solid carbon, and the device and the cyclone separation tube 5 are the same cavity. The evaporated salt gas can not block the air outlet pipe and can be attached to the inner wall of the sedimentation separator 4 to be a solid salt product again.
Specifically, the sedimentation separator 4 is used for separating gas-liquid-solid three-phase materials, and is obliquely arranged so that the recovered catalyst flows back into the reactor 1, the lower end of the sedimentation separator is communicated with the reactor 1, and the upper end of the sedimentation separator forms an air outlet end for outputting gas-phase materials; a salt charging port is arranged on the sedimentation separator 4; salt forms a salt layer in the sedimentation separator 4; the salt layer is used for separating solid-liquid two-phase materials. Wherein the main components of the solid-liquid two-phase material are a molten catalyst and a solid carbon product.
The salt feed port is arranged at the upper part of the sedimentation separator 4, and when molten catalyst and analysis gas (containing hydrogen generated after cracking and raw gas which is not completely cracked) pass through the spiral feeding device 3 and enter the cyclone separation pipe 5, salt starts to be added. When the spiral feeding device 3 is started, the salt adding is started in a chain manner; the salt adding mode is pneumatic conveying, and the salt adding amount is controlled by time.
The sedimentation separator 4 is obliquely arranged, and the inclination angle is preferably 30-60 degrees, so that sedimentation and reflux of the catalyst after passing through the salt layer are facilitated. The lower part of the sedimentation separator 4 is provided with a temperature control system, so that the temperature of the lower part of the sedimentation separator 4 is higher, and the temperature in the sedimentation separator 4 is reduced from bottom to top so as to keep the metal catalyst in a molten state to be settled at the bottom of the sedimentation separator. The tilt angle is designed to aid in the layered recovery of the material in combination with the density difference (catalyst density greater than salt density, salt density greater than solid carbon density). The molten metal catalyst decarbonized by the sedimentation separator 4 flows back to the reactor 1 through the flow control system 8 for recycling. Specifically, the flow control system 8 takes the density of the molten metal catalyst into consideration, and a buffer baffle and a flow control valve are arranged at the lower part of the sedimentation separator 4 to avoid damage to pipelines and equipment caused by the difference of flow states 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 be returned to the reactor 1 without bringing salts and carbon back into the reactor 1.
The middle part of the upper and lower interfaces (lower interface-interface with the reactor 1, upper interface-interface with the gas filter 6) of the sedimentation separator 4 is a material layer capable of effectively separating the catalyst and the solid carbon product, namely a salt layer, which is mostly inorganic salt, and the selected materials include but are not limited to: naCl, naBr, mnCl 2 KCl, etc.
The sedimentation separator 4 is provided with a catalyst feed inlet for supplementing catalyst, the catalyst feed inlet is positioned below the salt layer, and a fresh catalyst feed inlet is positioned at the middle lower part of the sedimentation separator 4, and the catalyst feed inlet is an important part for maintaining the activity of the catalyst according to the position adjustment of the catalyst feed inlet according to the change condition of the reaction.
The sedimentation separator 4 is also provided with a discharge opening 41 for discharging solid phase materials and salt layers. The separated salt and carbon are accumulated in the sedimentation separator 4, the carbon product can be continuously taken out, and after the reaction period is finished, the solid such as salt and carbon product is discharged after the system is stopped.
The reaction inner chamber of the sedimentation separator 4 is in a sealed state, so that volatile materials in a high temperature state, such as salt, can be effectively reduced and evaporated into an upstream pipeline and a downstream pipeline to form crystals, and blockage is caused.
Wherein, the principle of separating solid-liquid two-phase materials in a salt layer: 1) Because the density of the solid carbon is smaller than that of the salt layer and smaller than that of the catalyst, the density of the catalyst is larger than that of the salt layer, and the solid carbon, the salt layer and the catalyst are separated under the action of gravity; 2) Because the polarity of the catalyst is greater than that of the salt and the polarity of the salt is greater than that of the solid carbon, the salt becomes an effective medium for separating the catalyst from the carbon when the three are mixed. Based on any one of the above principles, the separation of solid-liquid two-phase materials in a salt layer can be realized.
A temperature control system for maintaining the catalyst in a molten state is provided at the end of the sedimentation separator 4 close to the reactor 1. According to the invention, the salt is added from the upper part in the settlement reaction, and the temperature of the lower part of the settlement separator 4 is used for keeping the molten state of the metal catalyst, so that the salt layer in direct contact with the catalyst is easier to be molten under the condition that the temperature is reduced from bottom to top, a physical interlayer can be naturally formed, the upward escape of metal steam can be effectively prevented, and the stability of the catalyst is increased.
The cyclone separation pipe 5 is arranged in the sedimentation separator 4 and is communicated with the output end of the spiral feeding device 3, the upper end of the cyclone separation pipe is communicated with the air outlet end of the sedimentation separator 4, and the lower end of the cyclone separation pipe is opened and is introduced into the salt layer, so that the molten catalyst and solid carbon in the cyclone separation pipe enter the salt layer. In particular, the lower part of the cyclone tube 5 extends deep into the middle salt layer 2/3 of the sedimentation separator 4.
Specifically, the cyclone separation tube 5 realizes gas-solid-liquid separation, adopts a structure with big top and small bottom, and preferably the material conveying tube is connected with the cyclone separation tube 5 in a tangential manner, so that the material is in a cyclone state in the tube, and the separation of gas-phase materials and liquid-solid-phase materials is facilitated. When the material enters the cyclone separation tube 5, the liquid-solid phase enters the sedimentation separator 4 downwards from the separation tube.
Specifically, the gas phase material upwards enters the upper part of the cyclone separation tube 5, and the gas phase material is filtered through the top of the cyclone separation tube 5 and then compressed into the PSA device for gas purification due to the sudden expansion of the tube diameter and the reduction of the flow velocity. The solid-liquid phase material enters the lower part of the cyclone separation pipe 5 downwards due to the gravity effect and finally enters the sedimentation separator 4.
For the escape of metal vapor which may occur during the reaction, the metal vapor can be condensed and refluxed into the sedimentation separator 4 due to the sudden expansion of the pipe diameter, the reduction of the flow speed and the lower temperature at the position.
And the gas filter 6 is communicated with the gas outlet end of the sedimentation separator 4 and is used for removing solid particles in the gas-phase material. Specifically, the high-temperature analysis gas (raw material gas containing hydrogen and having not been completely cracked) in the material passes through a gas filter 6, small amount of solid particles in the gas phase are removed, and then the gas flows into a high-temperature heat exchange module 7 to exchange heat with the unreacted raw material gas, so as to recover heat, and the gas enters PSA (Pressure Swing adsorption) after being cooled at a terminal, so as to purify the hydrogen.
The catalytic pyrolysis process of the flowable raw material gas for offshore facilities and ships comprises the following steps:
step 1, adding a catalyst from a catalyst feed inlet, and introducing the catalyst into a reactor 1 through a flow control system 8; the preheated feed gas is introduced into the reactor 1 through the distributor element 11 to start the catalytic cracking reaction. Generating gas-solid-liquid three phases in the reactor 1.
Step 2, starting a liquid level controller 2 and a spiral feeding device 3, wherein the liquid level controller 2 pushes gas-liquid-solid three-phase materials to enter the spiral feeding device 3; the gas-liquid-solid three-phase material enters the cyclone separation pipe 5 through the spiral feeding device 3.
And 3, enabling the gas-liquid-solid three-phase material to be in a rotational flow state in the rotational flow separation pipe 5, enabling the gas-liquid-solid three-phase material to enter the upper part of the rotational flow separation pipe 5 upwards, and separating the gas-phase material from the solid-liquid-phase material due to the fact that the pipe diameter of the rotational flow separation pipe 5 is enlarged, and the flow speed of the solid-liquid-phase material is reduced.
The gas phase material enters a gas filter 6 for filtering through the top of a cyclone separation pipe 5.
The solid-liquid phase material enters the lower part of the cyclone separation pipe 5 downwards due to the action of gravity and finally enters the salt layer of the sedimentation separator 4 through the lower end of the cyclone separation pipe 5.
And 4, separating the solid-phase material from the liquid-phase material in the salt layer.
And 5, refluxing the liquid phase material to the lower part of the sedimentation separator 4 after passing through the salt layer.
The foregoing is merely a preferred embodiment of the present invention and is not intended to limit the present invention in any way. Any person skilled in the art will make any equivalent substitution or modification to the technical solution and technical content disclosed in the invention without departing from the scope of the technical solution of the invention, and the technical solution of the invention is not departing from the scope of the invention.
Claims (6)
1. An offshore facility and marine flowable feed gas catalytic thermal cracking system comprising:
the reactor is used for carrying out catalytic reaction, a catalyst is placed in the reactor, and the raw material gas inlet end of the reactor is filled with raw material gas; the reactor is communicated with the output end of the sedimentation separator to recycle the catalyst in the sedimentation separator; the reactor is internally provided with a conveying pipe, one end of the conveying pipe, which extends out of the reactor, is communicated with the spiral feeding device, and one end of the conveying pipe, which is introduced into the reactor, is opened to receive gas-liquid-solid three-phase materials generated after catalytic reaction in the reactor;
the liquid level controller is used for conveying the gas-liquid-solid three-phase materials into the conveying pipe in a pressing mode;
the spiral feeding device is used for conveying the gas-liquid-solid three-phase materials into the sedimentation separator;
the sedimentation separator is used for separating gas-liquid-solid three-phase materials so that the recovered catalyst flows back into the reactor, the lower end of the sedimentation separator is communicated with the reactor, and the upper end of the sedimentation separator forms an air outlet end for outputting gas-phase materials; a salt feed inlet and a catalyst feed inlet are formed in the sedimentation separator; salt forms a salt layer in the sedimentation separator; the salt layer is used for separating solid-liquid two-phase materials; the separated carbon product is positioned above the salt layer, and the separated liquid regenerated catalyst is positioned below the salt layer; the catalyst charging port is positioned below the salt layer;
the cyclone separation pipe is arranged in the sedimentation separator and is communicated with the output end of the spiral feeding device, the upper end of the cyclone separation pipe is communicated with the air outlet end of the sedimentation separator, and the lower end of the cyclone separation pipe is opened and is led into the salt layer; the cyclone separation tube enables the molten catalyst and solid carbon in the cyclone separation tube to enter the salt layer;
a temperature control system is further provided to maintain the catalyst in a molten state, which is disposed at an end of the sedimentation separator near the reactor.
2. The offshore facility and marine flowable feed gas catalytic thermal cracking system of claim 1, wherein the settling separator is provided with a discharge port for discharging a portion of the carbon product and salt layer.
3. The offshore facility and marine flowable feed gas catalytic thermal cracking system of claim 1, further comprising a gas filter in communication with the outlet end of the settling separator for removing solid particles from the vapor phase material.
4. The offshore facility and marine flowable feed gas catalytic thermal cracking system of claim 3 further comprising a high temperature heat exchange module having an input in communication with the output of the gas filter for heat recovery.
5. The offshore facility and vessel catalytic pyrolysis system of claim 1 wherein the feed gas input to the reactor is provided with a gas distribution element.
6. A process for the catalytic pyrolysis of a flowable feed gas by means of an offshore installation and a marine catalytic pyrolysis system of a flowable feed gas according to any one of claims 1 to 5, comprising the steps of:
step 1, adding a catalyst into a reactor from a catalyst feed port; the preheated raw material gas is introduced into the reactor through the distributor element to start catalytic pyrolysis reaction; generating gas-solid-liquid three phases in the reactor;
step 2, starting a liquid level controller and a spiral feeding device, wherein the liquid level controller pushes the gas-liquid-solid three-phase material to enter the spiral feeding device; the gas-liquid-solid three-phase material enters a cyclone separation pipe through a spiral feeding device;
step 3, the gas-liquid-solid three-phase materials are in a cyclone state in the cyclone separation pipe, the gas-liquid-solid three-phase materials enter the upper part of the cyclone separation pipe upwards, and as the pipe diameter of the cyclone separation pipe is enlarged, the flow speed of the solid-liquid phase materials is reduced, and the gas-phase materials are separated from the solid-liquid phase materials;
the gas phase material enters a gas filter for filtration through the top of a cyclone separation pipe;
the solid-liquid phase material enters the lower part of the cyclone separation pipe downwards under the action of gravity and finally enters the salt layer of the sedimentation separator through the lower end of the cyclone separation pipe;
step 4, separating the solid phase material and the liquid phase material in a salt layer to obtain a solid carbon product;
and 5, refluxing the liquid phase material to a sedimentation separator after passing through a salt layer, and realizing continuous regeneration of the catalyst.
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| CN116712947A (en) | 2023-09-08 |
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