Plasma coupling thermocatalysis biomass gas phase online hydrogenation system and method

Abstract

The invention provides a plasma coupling thermocatalysis biomass gas phase on-line hydrogenation system and method.The plasma coupling thermocatalysis biomass gas phase on-line hydrogenation system mainly comprises a pyrolysis reaction system, an on-line hydrogenation system and a condensation system.The pyrolysis reaction system comprises a pyrolysis reactor and a pyrolysis gas outlet formed in the pyrolysis reactor; the pyrolysis reactor is used for carrying out pyrolysis reaction on biomass to generate pyrolytic carbon and pyrolysis gas, the pyrolysis gas is discharged through a pyrolysis gas outlet, the online hydrogenation system comprises a hydrogenation reactor, the hydrogenation reactor carries out online catalytic hydrogenation on the pyrolysis gas through hydrogen plasma and a catalyst to generate a hydrogenation product, and the condensation system comprises a condensation tank. And the condensation tank is used for condensing the hydrogenation product to obtain a condensed liquid product and non-condensed gas. According to the process, gas-phase online hydrogenation upgrading can be achieved, the active hydrogen plasma and the gas-phase pyrolysis product are subjected to the catalytic hydrogenation reaction at normal pressure, and compared with a traditional process, the process is small in overall loss and low in energy consumption, and operation is safer and more stable at normal pressure.

Description

Technical Field

[0001] The present invention relates to the technical field of biomass resource processing, and in particular to a plasma-coupled thermal catalytic biomass gas-phase online hydrogenation system and method. Background Art

[0002] Biomass is mainly composed of cellulose, hemicellulose and lignin. It is the only carbon-containing renewable resource with good high-value energy potential. Pyrolysis can upgrade biomass to produce three-phase products such as oil, gas and charcoal. It has many advantages such as strong raw material adaptability, fast reaction rate, less secondary pollution and self-sufficiency of energy. It is currently a relatively mature industrial disposal method. The gas phase volatiles of biomass pyrolysis are rich in oxygen-containing unsaturated components. Through reactions such as hydrogenation, deoxygenation and condensation, high-quality liquid fuels such as aromatics and paraffins can be prepared.

[0003] At present, the traditional biomass thermochemical process for preparing high-quality liquid fuels usually condenses the biomass pyrolysis products and then transfers the condensed bio-oil to a hydrothermal reaction system to synthesize the products. The hydrothermal process is a mixed reaction process of bio-oil, catalyst and water or organic solvent, and often requires further condensation, filtration, fractionation, extraction and other operations. The condensation and reheating process has high energy consumption, and the hydrothermal reaction hydrogenation process usually requires a pressure of several MPa to more than ten MPa. Therefore, the traditional process flow is long, the loss is large, and the risk level is high. Summary of the invention

[0004] In view of the deficiencies in the prior art, the purpose of the present invention is to provide a plasma-coupled thermal catalytic biomass gas-phase online hydrogenation system and method, which is mainly gas-phase online atmospheric pressure hydrogenation, using active hydrogen plasma and gas-phase pyrolysis products to undergo catalytic hydrogenation reactions, with lower overall losses and energy consumption, and atmospheric pressure operation is also safer.

[0005] In order to solve the above technical problems, the technical solution adopted by the present invention is:

[0006] A plasma-coupled thermal catalytic biomass gas-phase online hydrogenation system, comprising:

[0007] A pyrolysis reaction system, comprising a pyrolysis reactor and a pyrolysis gas outlet arranged on the pyrolysis reactor, wherein the pyrolysis reactor is used to perform a pyrolysis reaction on biomass to generate pyrolysis gas, and the pyrolysis gas is discharged through the pyrolysis gas outlet;

[0008] An online hydrogenation system comprises a hydrogenation reactor, wherein the hydrogenation reactor is provided with a hydrogenation reactant inlet, a catalyst inlet, a hydrogen plasma generator and a hydrogenation product outlet, wherein the hydrogenation reactant inlet is connected to the pyrolysis gas outlet via a pyrolysis gas discharge pipeline, the catalyst inlet is used to add a catalyst, the hydrogen plasma generator is used to generate hydrogen plasma, the hydrogenation reactor performs online catalytic hydrogenation and deoxygenation of the pyrolysis gas through hydrogen plasma and the catalyst to generate hydrogenation products and produce spent catalysts, and the hydrogenation product outlet is used to discharge the hydrogenation products;

[0009] The condensation system comprises a condensation tank, which is provided with a hydrogenation product inlet, a condensed liquid product outlet and a non-condensable gas outlet. The hydrogenation product inlet is connected to the hydrogenation product outlet. The condensation tank is used to condense the hydrogenation product to obtain a condensed liquid product and non-condensable gas. The condensed liquid product outlet is used to discharge the condensed liquid product, and the non-condensable gas outlet is used to discharge the non-condensable gas.

[0010] Furthermore, the hydrogen plasma generator is a plasma torch, which is provided with a hydrogen inlet and a plasma nozzle, the hydrogen inlet is used to introduce hydrogen, the plasma nozzle is arranged at the top of the hydrogenation reactor, the plasma torch is used to ionize hydrogen to generate hydrogen plasma, and the hydrogen plasma enters the hydrogenation reactor through the plasma nozzle.

[0011] Furthermore, a conical cavity is provided at the lower part of the hydrogenation reactor.

[0012] Furthermore, it also includes a first discharge pipe, the top of which is connected to the bottom of the hydrogenation reactor, a hydrogenation product outlet is arranged on the side of the first discharge pipe, and a spent catalyst outlet is arranged at the bottom of the first discharge pipe.

[0013] Furthermore, it also includes a second discharge pipe and a third discharge pipe, the hydrogenated product is divided into a first part and a second part, one end of the second discharge pipe is connected to the hydrogenated product outlet, and the other end of the second discharge pipe is connected to the hydrogenated product inlet, so that the first part of the hydrogenated product is discharged into the condensate tank, the second discharge pipe is provided with a circulating gas outlet, the pyrolysis gas discharge pipe is provided with a circulating gas inlet, one end of the third discharge pipe is connected to the circulating gas outlet, and the other end of the third discharge pipe is connected to the circulating gas inlet, so that the second part of the hydrogenated product enters the hydrogenation reactor for circulating hydrogenation.

[0014] Furthermore, a compression pump is provided on the third discharge pipeline, and the compression pump is used to extract the second portion of the hydrogenation product.

[0015] Furthermore, the pyrolysis gas outlet and the hydrogenation reactant inlet are connected via a pyrolysis gas exhaust pipe, and the other end of the third exhaust pipe is connected to the middle of the pyrolysis gas exhaust pipe to be connected to the hydrogenation reactant inlet.

[0016] Furthermore, it also includes a catalyst regeneration system, which includes a fourth discharge pipe and a catalyst regeneration reactor, one end of the fourth discharge pipe is connected to the bottom end of the first discharge pipe, and the other end of the fourth discharge pipe is connected to the catalyst regeneration reactor so that the spent catalyst is discharged into the catalyst regeneration reactor, the catalyst regeneration reactor is used to remove carbon deposits on the spent catalyst to generate a regenerated catalyst, and the catalyst regeneration reactor is connected to the hydrogenation reactor so that the regenerated catalyst is discharged into the hydrogenation reactor.

[0017] Furthermore, it also includes a cyclone separation system, which includes a cyclone separator, a hot air outlet, a gas-solid mixed flow inlet, a first regenerated catalyst outlet and a second regenerated catalyst outlet. The cyclone separator is used to separate the hot air mixed in the regenerated catalyst to air-dry the regenerated catalyst. The cyclone separator generates a first part of the regenerated catalyst and a second part of the regenerated catalyst. The catalyst regeneration reactor is provided with a gas-solid mixed flow outlet. The gas-solid mixed flow inlet is connected to the gas-solid mixed flow outlet through a fifth pipe to allow the regenerated catalyst to enter the cyclone separator. The hot air outlet is used to discharge hot air. The first regenerated catalyst outlet is connected to the hydrogenation reactor through a sixth discharge pipe to allow the first part of the regenerated catalyst to enter the hydrogenation reactor. The second regenerated catalyst outlet is used to discharge the first part of the regenerated catalyst.

[0018] A plasma-coupled thermal catalytic biomass gas-phase online hydrogenation method comprises the following steps:

[0019] Biomass pyrolysis: dry biomass raw materials and dry carrier gas are fed into the pyrolysis reactor, and biomass pyrolysis and heat self-supply are achieved by bottom ignition and air volume control, so that biomass pyrolysis produces pyrolysis gas and pyrolysis char, and the pyrolysis gas is discharged from the pyrolysis gas outlet;

[0020] Online hydrogenation of pyrolysis gas: pyrolysis gas enters the hydrogenation reactant from the hydrogenation reactant inlet through the pyrolysis gas discharge pipeline, the catalyst is added to the hydrogenation reactor from the catalyst inlet, hydrogen plasma is generated by the hydrogen plasma generator, and the pyrolysis gas is online catalytically hydrogenated and deoxygenated in the hydrogenation reactor by hydrogen plasma and catalyst to generate hydrogenation products and waste catalysts, and the hydrogenation product outlet is used to discharge the hydrogenation products;

[0021] Product condensation and separation: The hydrogenation product enters the condensation tank from the hydrogenation product inlet. The condensation tank is used to condense the hydrogenation product to obtain a condensed liquid product and a non-condensable gas. The condensed liquid product is discharged through the condensed liquid product outlet, and the non-condensable gas is discharged through the non-condensable gas outlet.

[0022] Compared with the prior art, the present invention has the following advantages and beneficial effects:

[0023] The plasma-coupled thermal catalytic biomass gas-phase online hydrogenation system and method provided by the present invention realizes the hydrogenation and deoxygenation of biomass pyrolysis gas in the atmospheric pressure gas phase by using hydrogen plasma as the reaction hydrogen source, thus solving the problems of long process flow, large loss and high energy consumption in the traditional process of condensing the biomass pyrolysis product into bio-oil and then further realizing hydrogenation and deoxygenation through a high-pressure hydrogenation system to prepare liquid fuel. At the same time, the online reaction is easy to control, which is convenient for realizing multi-reaction integration and easy to design a compact reactor. BRIEF DESCRIPTION OF THE DRAWINGS

[0024] The drawings described herein are used to provide a further understanding of the present invention and constitute a part of this application. The illustrative embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute an improper limitation of the present invention. In the drawings:

[0025] Figure 1 It is a schematic diagram of the plasma-coupled thermal catalytic biomass gas-phase online hydrogenation system of the present invention;

[0026] Figure 2 This is a schematic diagram of the first stereoscopic structure of the hydrogenation reactor of the present invention;

[0027] Figure 3 It is a schematic diagram of the second three-dimensional structure of the hydrogenation reactor of the present invention;

[0028] Figure 4 It is a logistics schematic diagram of the plasma coupled thermal catalytic biomass gas phase online hydrogenation method of the present invention;

[0029] Figure 5 The present invention is a process flow chart of the plasma coupled thermal catalytic biomass gas phase online hydrogenation method.

[0030] Among them, 1. pyrolysis reaction system; 101. pyrolysis reactor; 102. biomass feed port; 103. first gas inlet; 104. pyrolysis char outlet; 105. pyrolysis gas outlet;

[0031] 2. Online hydrogenation system; 201. Hydrogenation reactor; 202. Catalyst inlet; 203. Regenerated catalyst inlet; 204. Waste catalyst outlet; 205. Hydrogenation product outlet; 206. Hydrogen inlet; 207. Plasma torch; 208. Plasma nozzle; 209. Hydrogenation reactant inlet; 210. First discharge pipeline; 211. Circulating gas outlet; 212. Circulating gas inlet; 213. Compression pump; 214. Second discharge pipeline; 215. Third discharge pipeline; 216. Pyrolysis gas discharge pipeline;

[0032] 3. Condensation system; 301. Condensation tank; 302. Hydrogenation product inlet; 303. Incondensable gas outlet; 304. Condensate liquid product outlet;

[0033] 4. Catalyst regeneration system; 401. Catalyst regeneration reactor; 402. Regeneration gas-solid mixed flow outlet; 403. Waste catalyst inlet; 404. Second gas inlet; 405. Fourth discharge pipeline; 406. Fifth discharge pipeline; 407. Sixth discharge pipeline;

[0034] 5. Cyclone separation system; 501. Cyclone separator; 502. Hot air outlet; 503. Gas-solid mixed flow inlet; 504. First regenerated catalyst outlet; 505. Three-way valve; 506. First regenerated catalyst outlet. DETAILED DESCRIPTION

[0035] The technical solutions in the embodiments of the present invention will be described clearly and completely below in conjunction with the accompanying drawings in the embodiments of the present invention.

[0036] In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside" and the like indicate positions or positional relationships based on the positions or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as limiting the present invention. In addition, the terms "first", "second", and the like are only used for descriptive purposes, and cannot be understood as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, features defined as "first", "second", and the like may explicitly or implicitly include one or more of the features. In the description of the present invention, unless otherwise specified, "multiple" means two or more.

[0037] Example 1

[0038] In the related technology, the traditional biomass thermochemical process for preparing high-quality liquid fuels usually condenses the biomass pyrolysis products and then transfers the condensed bio-oil to a hydrothermal reaction system to synthesize the products. The hydrothermal process is a mixed reaction process of bio-oil, catalyst and water or organic solvent, and often requires further condensation, filtration, fractionation, extraction and other operations. The condensation and reheating process has high energy consumption, and the hydrothermal reaction hydrogenation process usually requires a pressure of several MPa to more than ten MPa. Therefore, the traditional process flow is long, the loss is large, and the risk level is high.

[0039] Example 1 provides a plasma-coupled thermal catalytic biomass gas-phase online hydrogenation system, in which biomass is subjected to a pyrolysis reaction by a pyrolysis reaction system 1 to generate pyrolysis gas, and then an online hydrogenation system 2 performs an online catalytic hydrogenation-deoxygenation reaction on the pyrolysis gas using a catalyst and hydrogen plasma, so that the pyrolysis gas generates a hydrogenation product, and then the hydrogenation product is condensed by a condensation system 3 to obtain a condensed liquid product and an incondensable gas, thereby realizing gas-phase online atmospheric pressure hydrogenation, using hydrogen plasma as a reaction hydrogen source and a catalytic hydrogenation reaction with the gas-phase pyrolysis product, with lower overall losses and energy consumption, and safer atmospheric pressure operation.

[0040] Example 1 provides a plasma coupled thermal catalytic biomass gas phase online hydrogenation system, such as Figure 1 As shown, it includes a pyrolysis reaction system 1, an online hydrogenation system 2 and a condensation system 3.

[0041] The pyrolysis reaction system 1 includes a pyrolysis reactor 101 and a pyrolysis gas outlet 105 disposed on the pyrolysis reactor 101 . The pyrolysis reactor 101 is used to perform a pyrolysis reaction on biomass to generate pyrolysis gas, and the pyrolysis gas is discharged through the pyrolysis gas outlet 105 .

[0042] The online hydrogenation system 2 includes a hydrogenation reactor 201, which is provided with a hydrogenation reactant inlet 209, a catalyst inlet 202, a hydrogen plasma generator and a hydrogenation product outlet 205. The hydrogenation reactant inlet 209 is connected to the pyrolysis gas outlet 105 through a pyrolysis gas exhaust pipe 216. The pyrolysis gas enters the hydrogenation reactor 201 from the hydrogenation reactant inlet 209 through the pyrolysis gas exhaust pipe 216. The catalyst inlet 202 is used to add a catalyst, and the hydrogen plasma generator is used to generate hydrogen plasma. The hydrogenation reactor 201 performs online catalytic hydrogenation and deoxygenation on the pyrolysis gas through hydrogen plasma and the catalyst to generate a hydrogenation product, and the hydrogenation product outlet 205 is used to discharge the hydrogenation product.

[0043] The condensation system 3 includes a condensation tank 301, which is provided with a hydrogenation product inlet 302, a condensed liquid product outlet 304 and a non-condensable gas outlet 303. The hydrogenation product inlet 302 is connected to the hydrogenation product outlet 205. The hydrogenation product enters the condensation tank 301 through the hydrogenation product inlet 302. The hydrogenation product inlet 302 is used to absorb the hydrogenation product. The condensation tank 301 is used to condense the hydrogenation product to obtain a condensed liquid product and non-condensable gas. The condensed liquid product outlet 304 is used to discharge the condensed liquid product, and the non-condensable gas outlet 303 is used to discharge the non-condensable gas.

[0044] The plasma-coupled thermal catalytic biomass gas-phase online hydrogenation system provided in this embodiment realizes the hydrogenation and deoxygenation of biomass pyrolysis gas in the gas phase by using hydrogen plasma as the reaction hydrogen source, thereby solving the problems of long process flow, large loss and high energy consumption in the traditional process of condensing biomass pyrolysis gas into bio-oil and then further realizing hydrogenation and deoxygenation through a high-pressure hydrogenation system to prepare liquid fuel. At the same time, the online reaction is easy to control, which is convenient for realizing multi-reaction integration and easy to design a compact reactor.

[0045] In this embodiment, Figure 1 As shown, the pyrolysis reactor 101 is also provided with a biomass feed port 102, a first gas inlet 103 and a pyrolysis charcoal outlet 104. The biomass feed port 102 is arranged at the top of the pyrolysis reactor 101. The biomass feed port 102 is used to enter biomass, and biomass includes but is not limited to straw, rice straw, wood chips, rice husks, etc., which are not limited in this embodiment. In the specific implementation of this embodiment, the biomass is rice straw. The biomass pyrolysis temperature is set to 400-800°C. In the specific implementation of this embodiment, the biomass pyrolysis temperature is set to 600°C. The heat is self-supplied by the heat in the pyrolysis reactor 101. The first gas inlet 103 is arranged on the side of the pyrolysis reactor 101. The first gas inlet 103 is used to add inert gas, commonly used nitrogen, argon, etc. or industrially available pyrolysis tail gas, and the pyrolysis charcoal outlet 104 is arranged at the bottom of the pyrolysis reactor 101. The pyrolysis charcoal outlet 104 is used to discharge pyrolysis charcoal.

[0046] In this embodiment, Figure 1 As shown, the hydrogen plasma generator is a plasma torch 207, which is provided with a hydrogen inlet 206 and a plasma nozzle 208. The hydrogen inlet 206 is used to introduce hydrogen, and the plasma nozzle 208 is arranged on the top of the hydrogenation reactor 201 to spray hydrogen into the hydrogenation reactor 201. The plasma torch 207 can be powered directly by the power grid or by local consumption of renewable energy power such as wind power, photovoltaic power, and hydropower.

[0047] The plasma torch 207 is equivalent to a plasma exciter, which can turn the material passing through it into a plasma state, and when hydrogen is introduced, hydrogen plasma will be ejected. The present invention sets the plasma torch 207 to ionize hydrogen to generate hydrogen plasma, and the hydrogen plasma enters the hydrogenation reactor 201 through the plasma nozzle 208.

[0048] In this embodiment, a conical cavity is provided at the lower part of the hydrogenation reactor 201. By providing the conical cavity at the lower part of the hydrogenation reactor 201, the catalyst will roll and sink in the reactor cavity due to different radial forces, which helps to reduce coking.

[0049] In this embodiment, Figure 2 and Figure 3 As shown, the hydrogenation reactor 201 includes a columnar cavity and a conical cavity arranged from top to bottom.

[0050] Specifically, in a specific implementation of this embodiment, Figure 2 and Figure 3 As shown, the cross section of the columnar cavity is circular or elliptical, and the conical cavity is a conical structure. In another specific implementation of this embodiment, the cross section of the columnar cavity is polygonal, and the conical cavity is a pyramidal structure, which is not limited in this embodiment. By adopting a conical or pyramidal structure at the lower part of the hydrogenation reactor 201, the catalyst can be rolled and sunk in the reactor, thereby alleviating the problem of catalyst carbon deposition and deactivation.

[0051] In this embodiment, the pyrolysis gas exhaust pipe 216 is a heat-insulating pipe, and the pyrolysis gas is kept warm through the pyrolysis gas exhaust pipe 216 .

[0052] In this embodiment, Figure 1-Figure 3 As shown, the catalyst inlet 202 is arranged at the top of the columnar cavity, and the catalyst inlet 202 is used to enter the catalyst. The types of catalysts added to the catalyst inlet include but are not limited to metal oxide catalysts, zeolite molecular sieve catalysts, etc., and different types of catalysts can be selected according to the target product requirements. The hydrogenation reactant inlet 209 is arranged on the side of the columnar cavity, and the hydrogenation product outlet 205 is arranged at the bottom of the conical cavity, and the hydrogenation product outlet 205 is used to discharge the hydrogenation product.

[0053] In this embodiment, Figure 1-Figure 3 As shown, the hydrogenation reactor 201 is provided with a spent catalyst outlet 204, which is disposed at the bottom of the hydrogenation reactor 201. Specifically, the spent catalyst outlet 204 is disposed at the bottom of the conical cavity, and the spent catalyst outlet 204 is used to discharge the spent catalyst.

[0054] Specifically, in this embodiment, Figure 1As shown, it also includes a first discharge pipe 210, the top of which is connected to the bottom of the hydrogenation reactor 201, a hydrogenation product outlet 205 is arranged on the side of the first discharge pipe 210, and a spent catalyst outlet 204 is arranged at the bottom of the first discharge pipe 210. The first discharge pipe 210 is vertically arranged so that solid particles (spent catalyst) sink and are discharged along the first discharge pipe 210, and the hydrogenation product (gaseous) is extracted through the side of the first discharge pipe 210.

[0055] In this embodiment, Figure 1 As shown, the second discharge pipe 214 and the third discharge pipe 215 are also included, and the hydrogenated product is divided into a first part and a second part. One end of the second discharge pipe 214 is connected to the hydrogenated product outlet 205, and the other end of the second discharge pipe 214 is connected to the hydrogenated product inlet 302, so that the first part of the hydrogenated product is discharged into the condensation tank 301. The second discharge pipe 214 is provided with a circulating gas outlet 211, and the pyrolysis gas discharge pipe 216 is provided with a circulating gas inlet 212. One end of the third discharge pipe 215 is connected to the circulating gas outlet 211, and the other end of the third discharge pipe 215 is connected to the circulating gas inlet 212, so that the second part of the hydrogenated product enters the hydrogenation reactor 201 for circulating hydrogenation.

[0056] In this embodiment, the second discharge pipe 214 is an insulation pipe for insulating the second portion of the hydrogenation product.

[0057] In this embodiment, the third discharge pipe 215 is an insulation pipe for insulating the second part of the hydrogenation product.

[0058] The present invention can circulate part of the hydrogenation product back to the hydrogenation reactor 201 to achieve secondary or multiple hydrogenation through bypass reflux circulation, thereby achieving cyclic hydrogenation, and can perform cyclic hydrogenation reaction on the pyrolysis gas that has not been completely reacted for the first time, thereby improving the overall conversion rate.

[0059] In this embodiment, Figure 1 As shown, a compression pump 213 is provided on the third discharge pipeline 215, and the compression pump 213 is used to extract the second part of the hydrogenation product, and cyclic hydrogenation is performed by extracting the second part of the hydrogenation product.

[0060] In this embodiment, the ratio of condensation and circulation of the hydrogenated product is controlled by the power of the compression pump 213 , wherein the circulation flow rate flowing through the circulation pump does not exceed 80% of the flow rate of the hydrogenated product flowing out of the hydrogenated product outlet 205 .

[0061] In this embodiment, Figure 1As shown, it also includes a catalyst regeneration system 4, which includes a fourth discharge pipe 405 and a catalyst regeneration reactor 401. One end of the fourth discharge pipe 405 is connected to the bottom end of the first discharge pipe 210, and the other end of the fourth discharge pipe 405 is connected to the catalyst regeneration reactor 401, so that the spent catalyst can be discharged into the catalyst regeneration reactor 401. The fourth discharge pipe 405 is inclined at a certain angle to facilitate the spent catalyst to slide into the catalyst regeneration reactor 401. The catalyst regeneration reactor 401 is used to remove carbon deposits on the spent catalyst to generate a regenerated catalyst. The catalyst regeneration reactor 401 is connected to the hydrogenation reactor 201 to discharge the regenerated catalyst into the hydrogenation reactor 201.

[0062] Specifically, Figure 1 As shown, the catalyst regeneration reactor 401 is provided with a regeneration gas-solid mixed flow outlet 402, a waste catalyst inlet 403 and a second gas inlet 404. The other end of the fourth discharge pipe 405 is connected to the waste catalyst inlet 403, so that the waste catalyst enters the catalyst regeneration reactor 401. The regeneration gas-solid mixed flow outlet 402 is used to discharge the regenerated catalyst mixed with hot air, and the second gas inlet 404 is used to allow air to enter.

[0063] The fourth discharge pipe 405 is a heat-insulating pipe, so as to ensure that the fourth discharge pipe 405 can keep the waste catalyst warm.

[0064] In this embodiment, Figure 1 As shown, a cyclone separation system 5 is also included. The cyclone separation system 5 is arranged between the catalyst regeneration reactor 401 and the hydrogenation reactor 201. The cyclone separation system 5 is used to separate the regenerated catalyst from the hot air.

[0065] Specifically, Figure 1 As shown, the cyclone separation system 5 includes a cyclone separator 501, the cyclone separation system 5 includes a cyclone separator 501, a hot air outlet 502, a gas-solid mixed flow inlet 503, a first regenerated catalyst outlet 504 and a second regenerated catalyst outlet 506, the cyclone separator 501 is used to separate the hot air mixed in the regenerated catalyst to air-dry the regenerated catalyst, the cyclone separator 501 generates a first part of the regenerated catalyst and a second part of the regenerated catalyst, a gas-solid mixed flow outlet is provided on the catalyst regeneration reactor 401, the gas-solid mixed flow inlet 503 is connected to the gas-solid mixed flow outlet through a fifth discharge pipe 406 to allow the regenerated catalyst to enter the cyclone separator 501, the hot air outlet 502 is used to discharge hot air, the first regenerated catalyst outlet 504 is connected to the regenerated catalyst inlet 203 provided on the hydrogenation reactor 201 through a sixth discharge pipe 407 to allow the first part of the regenerated catalyst to enter the hydrogenation reactor 201, and the first regenerated catalyst outlet 504 is used to discharge the second part of the regenerated catalyst.

[0066] In this embodiment, the sixth discharge pipe 407 is a heat-insulating pipe, so as to ensure that the sixth discharge pipe 407 can keep the first part of the regenerated catalyst warm.

[0067] In this embodiment, Figure 1 As shown, a three-way valve 505 is also included. A discharge port is arranged at the bottom of the cyclone separator 501. The first outlet of the three-way valve 505 is connected to the discharge port. The second outlet of the three-way valve 505 serves as a first regenerated catalyst outlet 504 to discharge the first part of the regenerated catalyst. The third outlet of the three-way valve 505 serves as a second regenerated catalyst outlet 506 to discharge the second part of the regenerated catalyst. The discharge time and flow rate of the first part of the regenerated catalyst and the second part of the regenerated catalyst can be determined by engineering effects.

[0068] In this embodiment, both liquid condensation products and non-condensable gases are effective products, among which pyrolytic carbon can be used to prepare carbon materials including but not limited to carbon fertilizer, activated carbon, carbon electrode carbon, etc., and liquid condensation products include but are not limited to one or more of aromatic hydrocarbons, chain alkanes, and olefins depending on the catalyst used. The non-condensable gas is mainly CO2, CO and a small amount of low-carbon hydrocarbons, which can be subsequently used as gas fuel or chemical raw materials, etc.

[0069] In this embodiment, the catalyst regeneration reactor 401 is a riser structure, which introduces air for combustion reaction and carries particles upward into the cyclone separation system 5. The carbon deposits on the spent catalyst are eliminated by combustion, and most of the heat generated by the combustion is carried by the hot catalyst particles into the hydrogenation reactor 201 to maintain the hydrogenation reaction temperature.

[0070] In this embodiment, the catalyst added into the catalyst inlet is a nickel-molybdenum oxide catalyst with granular titanium oxide as a carrier.

[0071] In this embodiment, the temperature of the online catalytic hydrodeoxygenation in the hydrogenation reactor 201 is 300-600° C., and the heat is supplied by the heat generated by the combustion in the catalyst regeneration reactor 401 through the regenerated catalyst.

[0072] In summary, the present invention utilizes the plasma torch 207 to excite hydrogen to generate high-energy active hydrogen plasma, and realizes the hydrodeoxygenation of biomass pyrolysis gas in the gas phase, thereby solving the problem of long process flow, large loss, and high energy consumption in the process of preparing liquid fuel by hydrodeoxygenation in the current high-pressure hydrogenation system after condensing the biomass pyrolysis gas into bio-oil in the traditional process. At the same time, the online reaction is easy to control, which is convenient for realizing multi-reaction integration and easy to design a compact reactor.

[0073] The present invention can achieve the utilization efficiency of the catalyst through the reactor structure design, wherein the lower part of the hydrogenation reactor 201 adopts a conical or pyramidal structure with an inclined angle, which can realize the rolling and sinking of the catalyst in the reactor, thereby alleviating the problem of catalyst carbon deposition and deactivation. The catalyst regeneration reactor 401 adopts a riser structure, which can eliminate the carbon deposition on the waste catalyst through combustion and bring it into the cyclone separator 501, and the separated catalyst particles can continue to be put into the hydrogenation reactor 201 for use.

[0074] The present invention can circulate part of the hydrogenation product back to the hydrogenation reactor 201 to achieve secondary or multiple hydrogenation by means of bypass reflux circulation, and can carry out cyclic hydrogenation reaction on the pyrolysis gas that has not been completely reacted for the first time, thereby improving the overall conversion rate. In addition, the catalyst can be recycled by means of riser combustion, the catalyst can be recycled, the amount of catalyst added to the catalyst inlet can be reduced, and the overall process economy can be improved.

[0075] The present invention realizes the self-supply of heat for the entire process by self-supplied heat from the biomass pyrolysis reactor 101 and heat from the catalyst regeneration process to the hydrogenation reactor 201, without the need for external heat supply. The plasma torch 207 used in the present invention can be powered not only by the power grid, but also by wind power, photovoltaic power, hydropower and other renewable energy power drive, so as to realize the instant local consumption of renewable energy power, solve the instability of renewable energy power, and further realize the clean and low-carbon overall process.

[0076] The present invention uses a conversion method of biomass pyrolysis and online hydrogenation of pyrolysis gas to obtain three-phase products of pyrolysis carbon, liquid fuel and other liquid products and carbon-containing non-condensable gas. Through catalyst design and adjustment of process parameters, it is possible to achieve the co-production of multiple target products or the directional preparation of a certain type of product, and realize the high-value resource utilization of biomass.

[0077] Example 2

[0078] Example 2 provides a plasma-coupled thermal catalytic biomass gas-phase online hydrogenation method, such as Figure 4 and Figure 5 As shown, the method is applied to the above-mentioned plasma coupled thermal catalytic biomass gas phase online hydrogenation system, comprising the following steps:

[0079] S1: Biomass pyrolysis: dry biomass raw materials and dry carrier gas are input into the pyrolysis reactor 101, and biomass pyrolysis and heat self-supply are achieved by bottom ignition and air volume control, so that the biomass is pyrolyzed to produce pyrolysis gas and pyrolysis char;

[0080] S2: Online hydrogenation of pyrolysis gas: The pyrolysis gas enters the hydrogenation reactant from the pyrolysis gas outlet 105 through the pyrolysis gas discharge pipe 216 and then from the hydrogenation reactant inlet 209, so that the catalyst enters the hydrogenation reactor 201 from the catalyst inlet 202, and hydrogen plasma is generated by the hydrogen plasma generator. The pyrolysis gas is subjected to online catalytic hydrogenation and deoxygenation in the hydrogenation reactor 201 by hydrogen plasma and catalyst to generate hydrogenation products and waste catalysts. The hydrogenation product outlet 205 is used to discharge the hydrogenation products;

[0081] S3: Product condensation and separation: The hydrogenation product is discharged from the hydrogenation product outlet 205 and then enters the condensation tank 301 through the hydrogenation product inlet 302. The condensation tank 301 is used to condense the hydrogenation product to obtain a condensed liquid product and a non-condensable gas. The condensed liquid product is discharged through the condensed liquid product outlet 304, and the non-condensable gas is discharged through the non-condensable gas outlet 303.

[0082] In this embodiment, when cyclic hydrogenation is required, step S4 is also included: product cyclic hydrogenation: the first part of the hydrogenation product discharged from the hydrogenation product outlet 205 enters the condensation tank 301 from the hydrogenation product inlet 302 through the second discharge pipe 214, and the second part of the hydrogenation product is pumped back to the hydrogenation reactant inlet 209 by the compression pump 213 arranged on the third discharge pipe 215, and enters the hydrogenation reactor 201 again to perform step S2.

[0083] In this embodiment, when a catalyst regeneration system 4 is provided, step S5 is also included: catalyst circulation regeneration: the waste catalyst enters the catalyst regeneration reactor 401 from the waste catalyst inlet 403 after passing through the first discharge pipe 210 and the fourth discharge pipe 405, and the air enters the catalyst regeneration reactor 401 from the second gas inlet 404. The waste catalyst particles and air undergo a combustion reaction, and the carbon deposits on the waste catalyst are removed. The gas-solid mixture enters the cyclone separator 501 from the regeneration gas-solid mixed flow outlet 402 to achieve gas-solid separation, and the hot air is discharged from the hot air outlet 502 at the upper end, and the regenerated catalyst is discharged from the first regenerated catalyst outlet 504, and enters the hydrogenation reactor 201 through the regenerated catalyst inlet 203 after passing through the sixth discharge pipe 407 to perform step S2.

[0084] In summary, this embodiment also discloses a plasma-coupled thermal catalytic biomass gas-phase online hydrogenation method, which generates high-energy active hydrogen plasma by driving the plasma torch 207 with renewable energy electricity, and combines the heat-assisted catalytic biomass pyrolysis gas generated during the catalyst regeneration process for online hydrogenation, thereby realizing the low-carbon and high-value conversion of biomass driven by renewable energy.

[0085] Obviously, those skilled in the art can make various changes and modifications to the present invention without departing from the spirit and scope of the present invention. Thus, if these modifications and variations of the present invention fall within the scope of the claims of the present invention and their equivalents, the present invention is also intended to include these modifications and variations.

Claims

1. A plasma coupled thermal catalytic biomass gas phase online hydrogenation system, characterized in that: include: A pyrolysis reaction system, comprising a pyrolysis reactor and a pyrolysis gas outlet arranged on the pyrolysis reactor, wherein the pyrolysis reactor is used to perform a pyrolysis reaction on biomass to generate pyrolysis gas, and the pyrolysis gas is discharged through the pyrolysis gas outlet; An online hydrogenation system comprises a hydrogenation reactor, wherein the hydrogenation reactor is provided with a hydrogenation reactant inlet, a catalyst inlet, a hydrogen plasma generator and a hydrogenation product outlet, wherein the hydrogenation reactant inlet is connected to the pyrolysis gas outlet via a pyrolysis gas discharge pipeline, the catalyst inlet is used to add a catalyst, the hydrogen plasma generator is used to generate hydrogen plasma, the hydrogenation reactor performs online catalytic hydrogenation and deoxygenation of the pyrolysis gas through hydrogen plasma and the catalyst to generate hydrogenation products and produce spent catalysts, and the hydrogenation product outlet is used to discharge the hydrogenation products; The condensation system comprises a condensation tank, which is provided with a hydrogenation product inlet, a condensed liquid product outlet and a non-condensable gas outlet. The hydrogenation product inlet is connected to the hydrogenation product outlet. The condensation tank is used to condense the hydrogenation product to obtain a condensed liquid product and non-condensable gas. The condensed liquid product outlet is used to discharge the condensed liquid product, and the non-condensable gas outlet is used to discharge the non-condensable gas.

2. The plasma coupled thermal catalytic biomass gas phase online hydrogenation system according to claim 1 is characterized by: The hydrogen plasma generator is a plasma torch, which is provided with a hydrogen inlet and a plasma nozzle. The hydrogen inlet is used to introduce hydrogen, and the plasma nozzle is arranged at the top of the hydrogenation reactor. The plasma torch is used to ionize hydrogen to generate hydrogen plasma, and the hydrogen plasma enters the hydrogenation reactor through the plasma nozzle.

3. The plasma coupled thermal catalytic biomass gas phase online hydrogenation system according to claim 1 is characterized by: A conical cavity is arranged at the lower part of the hydrogenation reactor.

4. The plasma coupled thermal catalytic biomass gas phase online hydrogenation system according to claim 1, characterized in that: It also includes a first discharge pipe, the top of which is connected to the bottom of the hydrogenation reactor, a hydrogenation product outlet is arranged on the side of the first discharge pipe, and a spent catalyst outlet is arranged at the bottom of the first discharge pipe.

5. The plasma coupled thermal catalytic biomass gas phase online hydrogenation system according to claim 4 is characterized in that: It also includes a second discharge pipe and a third discharge pipe, the hydrogenated product is divided into a first part and a second part, one end of the second discharge pipe is connected to the hydrogenated product outlet, and the other end of the second discharge pipe is connected to the hydrogenated product inlet, so that the first part of the hydrogenated product is discharged into the condensate tank, the second discharge pipe is provided with a circulating gas outlet, the pyrolysis gas discharge pipe is provided with a circulating gas inlet, one end of the third discharge pipe is connected to the circulating gas outlet, and the other end of the third discharge pipe is connected to the circulating gas inlet, so that the second part of the hydrogenated product enters the hydrogenation reactor for circulating hydrogenation.

6. The plasma coupled thermal catalytic biomass gas phase online hydrogenation system according to claim 5, characterized in that: The third discharge pipeline is provided with a compression pump, and the compression pump is used to extract the second portion of the hydrogenation product.

7. The plasma coupled thermal catalytic biomass gas phase online hydrogenation system according to claim 4 is characterized by: The pyrolysis gas outlet and the hydrogenation reactant inlet are connected through a pyrolysis gas exhaust pipe, and the other end of the third exhaust pipe is connected to the middle of the pyrolysis gas exhaust pipe to be connected to the hydrogenation reactant inlet.

8. The plasma coupled thermal catalytic biomass gas phase online hydrogenation system according to claim 4 is characterized by: It also includes a catalyst regeneration system, which includes a fourth discharge pipe and a catalyst regeneration reactor, one end of the fourth discharge pipe is connected to the bottom end of the first discharge pipe, and the other end of the fourth discharge pipe is connected to the catalyst regeneration reactor so that the spent catalyst is discharged into the catalyst regeneration reactor, the catalyst regeneration reactor is used to remove carbon deposits on the spent catalyst to generate a regenerated catalyst, and the catalyst regeneration reactor is connected to the hydrogenation reactor so that the regenerated catalyst is discharged into the hydrogenation reactor.

9. The plasma coupled thermal catalytic biomass gas phase online hydrogenation system according to claim 8, characterized in that: It also includes a cyclone separation system, which includes a cyclone separator, a hot air outlet, a gas-solid mixed flow inlet, a first regenerated catalyst outlet and a second regenerated catalyst outlet. The cyclone separator is used to separate the hot air mixed in the regenerated catalyst to air-dry the regenerated catalyst. The cyclone separator generates a first part of the regenerated catalyst and a second part of the regenerated catalyst. The catalyst regeneration reactor is provided with a gas-solid mixed flow outlet. The gas-solid mixed flow inlet is connected to the gas-solid mixed flow outlet through a fifth pipe to allow the regenerated catalyst to enter the cyclone separator. The hot air outlet is used to discharge hot air. The first regenerated catalyst outlet is connected to the hydrogenation reactor through a sixth discharge pipe to allow the first part of the regenerated catalyst to enter the hydrogenation reactor. The second regenerated catalyst outlet is used to discharge the first part of the regenerated catalyst.

10. A plasma-coupled thermal catalytic biomass gas phase online hydrogenation method, characterized in that: The following steps are involved: Biomass pyrolysis: dry biomass raw materials and dry carrier gas are fed into the pyrolysis reactor, and biomass pyrolysis and heat self-supply are achieved by bottom ignition and air volume control, so that biomass pyrolysis produces pyrolysis gas and pyrolysis char, and the pyrolysis gas is discharged from the pyrolysis gas outlet; Online hydrogenation of pyrolysis gas: pyrolysis gas enters the hydrogenation reactant from the hydrogenation reactant inlet through the pyrolysis gas discharge pipeline, the catalyst is added to the hydrogenation reactor from the catalyst inlet, hydrogen plasma is generated by the hydrogen plasma generator, and the pyrolysis gas is online catalytically hydrogenated and deoxygenated in the hydrogenation reactor by hydrogen plasma and catalyst to generate hydrogenation products and waste catalysts, and the hydrogenation product outlet is used to discharge the hydrogenation products; Product condensation and separation: The hydrogenation product enters the condensation tank from the hydrogenation product inlet. The condensation tank is used to condense the hydrogenation product to obtain a condensed liquid product and a non-condensable gas. The condensed liquid product is discharged through the condensed liquid product outlet, and the non-condensable gas is discharged through the non-condensable gas outlet.

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