In-situ hydrogenation system and method for biomass gas phase by means of plasma-coupled thermal catalysis

Abstract

Provided in the present invention are an in-situ hydrogenation system and method for a biomass gas phase by means of a plasma-coupled thermal catalysis. The in-situ hydrogenation system mainly comprises a pyrolysis reaction system, an in-situ hydrogenation system and a condensation system, wherein the pyrolysis reaction system comprises a pyrolysis reactor and a pyrolysis gas outlet provided on the pyrolysis reactor, the pyrolysis reactor being configured to perform a pyrolysis reaction on biomass to generate pyrolysis char and pyrolysis gas which is discharged through the pyrolysis gas outlet; the in-situ hydrogenation system comprises a hydrogenation reactor, the hydrogenation reactor performing in-situ catalytic hydrogenation on the pyrolysis gas by means of hydrogen plasma and a catalyst to generate a hydrogenation product; and the condensation system comprises a condensation tank configured to condense the hydrogenation product to obtain a condensed liquid product and non-condensed gas. The present invention can achieve gas-phase in-situ hydrogenation upgrading, and a catalytic hydrogenation reaction occurs at atmospheric pressure by means of active hydrogen plasma and a gas-phase pyrolysis product; and compared with a traditional process, the process of the present invention has a smaller overall loss and low energy consumption, and operates more safely and stably at atmospheric pressure.

Description

Plasma-coupled thermal catalytic biomass gas-phase online hydrogenation system and method TECHNICAL FIELD

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

[0002] Biomass is mainly composed of cellulose, hemicellulose and lignin, and is the only carbon-containing renewable resource, which has good high-value energy potential. Pyrolysis can upgrade biomass to produce oil, gas and carbon, etc. three-phase products, which has many advantages such as strong adaptability of raw materials, fast reaction rate, less secondary pollution, energy self-supply, etc. It is a relatively mature industrialized disposal method. The gas-phase volatile components of biomass pyrolysis are rich in oxygen-containing unsaturated components, which can be prepared into aromatic hydrocarbons, alkanes and other high-quality liquid fuels through hydrogenation and deoxygenation and condensation reactions.

[0003] At present, the traditional biomass thermochemical preparation of high-quality liquid fuel process usually condenses the biomass pyrolysis products, and then transfers the condensed bio-oil to a hydrothermal reaction system to synthesize products. The hydrothermal process is a mixed reaction process of bio-oil, catalyst and water or organic solvent, and further condensation, filtration, fractionation, extraction and other operations are often required. The condensation and heating process has high energy consumption, and the hydrothermal reaction hydrogenation process usually requires several to tens of megapascals of pressure. Therefore, the traditional process flow is long, the loss is large, and the danger is high.

[0004] SUMMARY

[0005] In view of the deficiencies of the prior art, the present application provides a plasma-coupled thermal catalytic biomass gas-phase online hydrogenation system and method, which is mainly a gas-phase online atmospheric hydrogenation. The active hydrogen plasma and the gas-phase pyrolysis products undergo catalytic hydrogenation reaction, the overall loss and energy consumption are lower, and the atmospheric operation is also safer.

[0006] In order to solve the above technical problems, the technical scheme adopted by the present application is:

[0007] A plasma-coupled thermal catalytic biomass gas-phase online hydrogenation system, comprising:

[0008] A pyrolysis reaction system comprising a pyrolysis reactor and a pyrolysis gas outlet provided on the pyrolysis reactor, the pyrolysis reactor being used for pyrolysis reaction of biomass to produce pyrolysis gas, and the pyrolysis gas being discharged through the pyrolysis gas outlet;

[0009] An online hydrogenation system, comprising a hydrogenation reactor, wherein a hydrogenation reactant inlet, a catalyst inlet, a hydrogen plasma generator and a hydrogenation product outlet are arranged on the hydrogenation reactor, the hydrogenation reactant inlet is connected with the pyrolysis gas outlet through a pyrolysis gas discharge pipeline, the catalyst inlet is used for adding catalyst, the hydrogen plasma generator is used for generating hydrogen plasma, the hydrogenation reactor is used for generating hydrogenation product and waste catalyst by online catalytic hydrogenation deoxidization of the pyrolysis gas through the hydrogen plasma and the catalyst, and the hydrogenation product outlet is used for discharging the hydrogenation product;

[0010] A condensing system, comprising a condensing tank, wherein a hydrogenation product inlet, a condensed liquid product outlet and a non-condensed gas outlet are arranged on the condensing tank, the hydrogenation product inlet is communicated with the hydrogenation product outlet, the condensing tank is used for condensing the hydrogenation product to obtain condensed liquid product and non-condensed gas, the condensed liquid product outlet is used for discharging the condensed liquid product, and the non-condensed gas outlet is used for discharging the non-condensed gas.

[0011] Further, the hydrogen plasma generator is a plasma torch, wherein a hydrogen inlet and a plasma jet are arranged on the plasma torch, the hydrogen inlet is used for introducing hydrogen, the plasma jet is arranged at the top of the hydrogenation reactor, the plasma torch is used for ionizing hydrogen to generate hydrogen plasma, and the hydrogen plasma enters the hydrogenation reactor through the plasma jet.

[0012] Further, a conical cavity is arranged at the lower part of the hydrogenation reactor.

[0013] Further, a first discharge pipeline is arranged, wherein the top end of the first discharge pipeline is communicated with the bottom of the hydrogenation reactor, the side of the first discharge pipeline is provided with a hydrogenation product outlet, and the bottom end of the first discharge pipeline is provided with a waste catalyst outlet.

[0014] Further, a second discharge pipeline and a third discharge pipeline are arranged, the hydrogenation product is divided into a first part and a second part, one end of the second discharge pipeline is connected with the hydrogenation product outlet, the other end of the second discharge pipeline is connected with the hydrogenation product inlet, so that the first part of the hydrogenation product is discharged into the condensing tank, a circulating gas outlet is arranged on the second discharge pipeline, a circulating gas inlet is arranged on the pyrolysis gas discharge pipeline, one end of the third discharge pipeline is connected with the circulating gas outlet, and the other end of the third discharge pipeline is connected with the circulating gas inlet, so that the second part of the hydrogenation product enters the hydrogenation reactor for cyclic hydrogenation.

[0015] Further, a compression pump is arranged on the third discharge pipeline, and the compression pump is used for pumping out the second part of the hydrogenation product.

[0016] Further, the pyrolysis gas outlet and the hydrogenation reactant inlet are connected by a pyrolysis gas discharge pipeline, the other end of the third discharge pipeline is connected with the middle part of the pyrolysis gas discharge pipeline to be connected with the hydrogenation reactant inlet.

[0017] Further, a catalyst regeneration system is further included, the catalyst regeneration system includes a fourth discharge pipeline and a catalyst regeneration reactor, one end of the fourth discharge pipeline is connected with the bottom end of the first discharge pipeline, and the other end of the fourth discharge pipeline is connected with the catalyst regeneration reactor to discharge the waste catalyst into the catalyst regeneration reactor, the catalyst regeneration reactor is used to remove the carbon deposit on the waste catalyst to generate regenerated catalyst, and the catalyst regeneration reactor is connected with the hydrogenation reactor to discharge the regenerated catalyst into the hydrogenation reactor.

[0018] Further, a cyclone separation system is further included, the cyclone separation system 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 mixed hot air in the regenerated catalyst to 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 with the gas-solid mixed flow outlet by a fifth pipeline to make the regenerated catalyst enter into the cyclone separator, the hot air outlet is used to discharge the hot air, the first regenerated catalyst outlet is connected with the hydrogenation reactor by a sixth discharge pipeline to make the first part of the regenerated catalyst enter into the hydrogenation reactor, and the second regenerated catalyst outlet is used to discharge the first part of the regenerated catalyst.

[0019] A plasma-coupled thermal catalytic biomass gas phase online hydrogenation method, comprising the following steps:

[0020] Biomass pyrolysis: dry biomass raw materials and dry carrier gas are input into a pyrolysis reactor, biomass pyrolysis and heat self-supply are realized by bottom ignition and control of air volume, biomass pyrolysis generates pyrolysis gas and pyrolysis carbon, and the pyrolysis gas is discharged from a pyrolysis gas outlet;

[0021] Pyrolysis gas online hydrogenation: the pyrolysis gas enters into a hydrogenation reactant from a hydrogenation reactant inlet through a pyrolysis gas discharge pipeline, the catalyst is added into the hydrogenation reactor from a catalyst inlet, hydrogen plasma is generated by a hydrogen plasma generator, the pyrolysis gas is catalytically hydrogenated and deoxidized in the hydrogenation reactor by the hydrogen plasma and the catalyst to generate hydrogenation products and waste catalyst, and a hydrogenation product outlet is used to discharge the hydrogenation products;

[0022] The hydrogenation product enters a condensation tank from a hydrogenation product inlet, the condensation tank is used for condensing the hydrogenation product to obtain a condensed liquid product and non-condensed gas, the condensed liquid product is discharged through a condensed liquid product outlet, and the non-condensed gas is discharged through a non-condensed gas outlet.

[0023] Compared with the prior art, the present application has the following advantages and beneficial effects:

[0024] The present application provides a kind of plasma coupling thermal catalytic biomass gas phase on-line hydrogenation system and method, by utilizing hydrogen plasma as reaction hydrogen source, realizes the hydrogenation of biomass pyrolysis gas in normal pressure gas phase, solves the problems of long process, large loss and high energy consumption in the process of preparing liquid fuel by hydrogenation deoxidation of biomass pyrolysis product condensed into bio-oil and then further through high pressure hydrogenation system. BRIEF DESCRIPTION OF DRAWINGS

[0025] The drawings described herein are used to provide further understanding of the present application, and constitute a part of the present application. The illustrative embodiments of the present application and their descriptions are used to explain the present application, and do not constitute an improper limitation on the present application. In the drawings:

[0026] Fig. 1 is a schematic diagram of the plasma coupling thermal catalytic biomass gas phase on-line hydrogenation system of the present application;

[0027] Fig. 2 is a first kind of schematic diagram of the hydrogenation reactor of the present application;

[0028] Fig. 3 is a second kind of schematic diagram of the hydrogenation reactor of the present application;

[0029] Fig. 4 is a schematic diagram of the material flow of the plasma coupling thermal catalytic biomass gas phase on-line hydrogenation method of the present application;

[0030] Fig. 5 is a process flow diagram of the plasma coupling thermal catalytic biomass gas phase on-line hydrogenation method of the present application.

[0031] 1, pyrolysis reaction system; 101, pyrolysis reactor; 102, biomass feed inlet; 103, first gas inlet; 104, pyrolysis carbon outlet; 105, pyrolysis gas outlet;

[0032] 2, on-line hydrogenation system; 201, hydrogenation reactor; 202, catalyst inlet; 203, regenerated catalyst inlet; 204, spent catalyst outlet; 205, hydrogenation product outlet; 206, hydrogen inlet; 207, plasma torch; 208, plasma jet; 209, hydrogenation reactant inlet; 210, first exhaust conduit; 211, recycle gas outlet; 212, recycle gas inlet; 213, compression pump; 214, second exhaust conduit; 215, third exhaust conduit; 216, pyrolysis gas exhaust conduit;

[0033] 3, condensation system; 301, condensation tank; 302, hydrogenation product inlet; 303, non-condensed gas outlet; 304, condensed liquid product outlet;

[0034] 4, catalyst regeneration system; 401, catalyst regeneration reactor; 402, regenerated gas-solid mixture outlet; 403, spent catalyst inlet; 404, second gas inlet; 405, fourth exhaust conduit; 406, fifth exhaust conduit; 407, sixth exhaust conduit;

[0035] 5, cyclone separation system; 501, cyclone separator; 502, hot air outlet; 503, gas-solid mixture inlet; 504, first regenerated catalyst outlet; 505, three-way valve; 506, first regenerated catalyst outlet. DETAILED DESCRIPTION

[0036] The technical solutions in the embodiments of the present application will be clearly and completely described in connection with the drawings in the embodiments of the present application.

[0037] In the description of the present application, it should be understood that the terms "center", "longitudinal", "transverse", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer" and the like indicate the orientation or positional relationship based on the orientation or positional relationship shown in the drawings, and are only for the purpose of facilitating the description of the present application and simplifying the description, and do not indicate or imply that the device or element referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore cannot be understood as a limitation of the present application. In addition, the terms "first", "second" and the like are only for the purpose of description and cannot be understood as indicating or implying relative importance or implicitly indicating the number of the technical features indicated. Therefore, the features defined with "first", "second" and the like can explicitly or implicitly include one or more of the features. In the description of the present application, unless otherwise specified, the meaning of "a plurality of" is two or more.

[0038] Example 1

[0039] In the related art, the traditional biomass thermo-chemical preparation of high-quality liquid fuel process usually condenses the pyrolysis products of biomass, and then transfers the condensed bio-oil to a hydrothermal reaction system to synthesize products. The hydrothermal process is a mixed reaction process of bio-oil, catalyst and water or organic solvent, and further condensation, filtration, fractionation, extraction and other operations are often required. The condensation and reheating process has high energy consumption, and the hydrothermal reaction and hydrogenation process usually requires a pressure of several to tens of megapascals. Therefore, the traditional process has a long process flow, high loss and high risk.

[0040] Embodiment 1 provides a plasma-coupled thermal catalytic biomass gas-phase online hydrogenation system. The biomass is pyrolyzed by a pyrolysis reaction system 1 to produce pyrolysis gas, and then the pyrolysis gas is subjected to online catalytic hydrogenation and deoxidation reaction by a catalyst and hydrogen plasma in an online hydrogenation system 2 to produce hydrogenation products. The hydrogenation products are condensed by a condensation system 3 to obtain condensed liquid products and non-condensed gas. Thus, gas-phase online atmospheric hydrogenation can be realized, and the hydrogen plasma is used as the reaction hydrogen source to react with the gas-phase pyrolysis products. The overall loss and energy consumption are lower, and the atmospheric operation is safer.

[0041] Embodiment 1 provides a plasma-coupled thermal catalytic biomass gas-phase online hydrogenation system, as shown in FIG. 1, which includes a pyrolysis reaction system 1, an online hydrogenation system 2 and a condensation system 3.

[0042] The pyrolysis reaction system 1 includes a pyrolysis reactor 101 and a pyrolysis gas outlet 105 arranged on the pyrolysis reactor 101. The pyrolysis reactor 101 is used for pyrolyzing biomass to produce pyrolysis gas, and the pyrolysis gas is discharged through the pyrolysis gas outlet 105.

[0043] The online hydrogenation system 2 includes a hydrogenation reactor 201, and the hydrogenation reactor 201 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 discharge pipeline 216. The pyrolysis gas enters the hydrogenation reactor 201 from the hydrogenation reactant inlet 209 through the pyrolysis gas discharge pipeline 216. The catalyst inlet 202 is used for adding catalyst. The hydrogen plasma generator is used for generating hydrogen plasma. The hydrogenation reactor 201 generates hydrogenation products by online catalytic hydrogenation and deoxidation of the pyrolysis gas through hydrogen plasma and catalyst. The hydrogenation product outlet 205 is used for discharging hydrogenation products.

[0044] The condensing system 3 comprises a condensing tank 301, which is provided with a hydrogenated product inlet 302, a condensed liquid product outlet 304 and a non-condensed gas outlet 303. The hydrogenated product inlet 302 is communicated with the hydrogenated product outlet 205, and the hydrogenated product enters the condensing tank 301 through the hydrogenated product inlet 302. The hydrogenated product inlet 302 is used for absorbing the hydrogenated product. The condensing tank 301 is used for condensing the hydrogenated product to obtain condensed liquid product and non-condensed gas. The condensed liquid product outlet 304 is used for discharging the condensed liquid product. The non-condensed gas outlet 303 is used for discharging the non-condensed gas.

[0045] The embodiment provides a plasma-coupled thermal catalytic biomass gas-phase online hydrogenation system. Hydrogen plasma is used as a reaction hydrogen source to realize hydrogenation and deoxidation of biomass pyrolysis gas in a gas phase, so that the problems of long process flow, great loss and high energy consumption in the process of preparing liquid fuel by hydrogenation and deoxidation of the biomass pyrolysis gas condensed into bio-oil through a high-pressure hydrogenation system in the traditional process are solved. The online reaction is easy to control, and is convenient for realizing multi-reaction integration and designing a compact reactor.

[0046] In the embodiment, as shown in FIG. 1, the pyrolysis reactor 101 is further provided with a biomass feeding port 102, a first gas inlet 103 and a pyrolysis carbon outlet 104. The biomass feeding port 102 is arranged at the top of the pyrolysis reactor 101, and is used for feeding biomass. The biomass includes, but is not limited to, straw, rice straw, sawdust, rice husk and the like, and the embodiment is not limited thereto. In the specific embodiment of the embodiment, the biomass is rice straw. The biomass pyrolysis temperature is set to 400-800 DEG C, and in the specific embodiment of the embodiment, the biomass pyrolysis temperature is set to 600 DEG C. The heat is self-supplied in the pyrolysis reactor 101. The first gas inlet 103 is arranged on the side of the pyrolysis reactor 101, and is used for adding inert gas, commonly nitrogen, argon or tail gas available for pyrolysis in industry. The pyrolysis carbon outlet 104 is arranged at the bottom of the pyrolysis reactor 101, and is used for discharging pyrolysis carbon.

[0047] In the embodiment, as shown in FIG. 1, the hydrogen plasma generator is a plasma torch 207, which is provided with a hydrogen inlet 206 and a plasma jet 208. The hydrogen inlet 206 is used for introducing hydrogen. The plasma jet 208 is arranged at the top of the hydrogenation reactor 201 and is used for spraying hydrogen into the hydrogenation reactor 201. The plasma torch 207 can be directly powered by the power grid or by renewable energy power such as wind power, photovoltaic power and hydroelectric power.

[0048] The plasma torch 207 corresponds to a plasma exciter, which can change the material passing through it into a plasma state, and when hydrogen gas is passed through it, hydrogen plasma is sprayed out. The present application provides the plasma torch 207 for ionizing hydrogen gas to generate hydrogen plasma, and the hydrogen plasma enters the hydrogenation reactor 201 through the plasma nozzle 208.

[0049] In the embodiment, the hydrogenation reactor 201 is provided with a conical cavity at the lower part, and the catalyst will roll and sink in the reactor cavity due to different radial forces, which helps to reduce coking.

[0050] In the embodiment, as shown in FIGS. 2 and 3, the hydrogenation reactor 201 comprises a cylindrical cavity and a conical cavity arranged from top to bottom.

[0051] Specifically, in one specific embodiment of the present application, as shown in FIGS. 2 and 3, the cross section of the cylindrical cavity is circular or elliptical, and the conical cavity is a conical structure. In another specific embodiment of the present application, the cross section of the cylindrical cavity is polygonal, and the conical cavity is a pyramidal structure. The present application is not limited in this regard. By using a conical or pyramidal structure at the lower part of the hydrogenation reactor 201, the catalyst can roll and sink in the reactor, thereby alleviating the problem of catalyst carbon deposition and deactivation.

[0052] In the embodiment, the pyrolysis gas discharge pipeline 216 is a heat preservation pipeline, and the pyrolysis gas is heat preserved through the pyrolysis gas discharge pipeline 216.

[0053] In the embodiment, as shown in FIGS. 1-3, the catalyst inlet 202 is arranged at the top of the cylindrical cavity, and the catalyst inlet 202 is used for entering the catalyst. The types of catalyst added by the catalyst inlet include but are not limited to metal oxide catalyst, zeolite molecular sieve catalyst, etc., and different types of catalysts can be selected according to the demand of target product. The hydrogenation reactant inlet 209 is arranged on the side of the cylindrical cavity, and the hydrogenation product outlet 205 is arranged at the bottom of the conical cavity. The hydrogenation product outlet 205 is used for discharging the hydrogenation product.

[0054] In the embodiment, as shown in FIGS. 1-3, the hydrogenation reactor 201 is provided with a waste catalyst outlet 204, and the waste catalyst outlet 204 is arranged at the bottom of the hydrogenation reactor 201. Specifically, the waste catalyst outlet 204 is arranged at the bottom of the conical cavity, and the waste catalyst outlet 204 is used for discharging the waste catalyst.

[0055] Specifically, as shown in FIG. 1, the first discharge pipeline 210 is further included in the embodiment, a top end of the first discharge pipeline 210 is communicated with a bottom of the hydrogenation reactor 201, a side of the first discharge pipeline 210 is provided with the hydrogenation product outlet 205, a bottom end of the first discharge pipeline 210 is provided with the waste catalyst outlet 204, the first discharge pipeline 210 is vertically arranged to make the solid particles (waste catalyst) sink and discharge along the first discharge pipeline 210, and the hydrogenation product (gaseous) is extracted through the side of the first discharge pipeline 210.

[0056] As shown in FIG. 1, the second discharge pipeline 214 and the third discharge pipeline 215 are further included in the embodiment, the hydrogenation product is divided into a first part and a second part, one end of the second discharge pipeline 214 is connected with the hydrogenation product outlet 205, the other end of the second discharge pipeline 214 is connected with the hydrogenation product inlet 302, so that the first part of the hydrogenation product is discharged into the condensing tank 301. The circulating gas outlet 211 is arranged on the second discharge pipeline 214, and the circulating gas inlet 212 is arranged on the pyrolysis gas discharge pipeline 216. One end of the third discharge pipeline 215 is connected with the circulating gas outlet 211, and the other end of the third discharge pipeline 215 is connected with the circulating gas inlet 212, so that the second part of the hydrogenation product enters the hydrogenation reactor 201 to perform the circulating hydrogenation.

[0057] In the embodiment, the second discharge pipeline 214 is a heat preservation pipeline, which is used for heat preservation of the second part of the hydrogenation product.

[0058] In the embodiment, the third discharge pipeline 215 is a heat preservation pipeline, which is used for heat preservation of the second part of the hydrogenation product.

[0059] The present application can realize secondary or multiple hydrogenation by returning part of the hydrogenation product to the hydrogenation reactor 201 through the bypass reflux circulation, and further realize the circulating hydrogenation, so that the pyrolysis gas which is not completely reacted in the first time can be subjected to the circulating hydrogenation reaction, thereby improving the overall conversion rate.

[0060] As shown in FIG. 1, the third discharge pipeline 215 is provided with the compression pump 213 in the embodiment, the compression pump 213 is used for extracting the second part of the hydrogenation product to perform the circulating hydrogenation.

[0061] In the embodiment, the ratio of the hydrogenation product condensation and circulation is controlled by the power of the compression pump 213, and the circulating flow rate of the circulating pump is not more than 80% of the flow rate of the hydrogenation product discharged from the hydrogenation product outlet 205.

[0062] In the embodiment, as shown in FIG. 1, the catalyst regeneration system 4 is further included, the catalyst regeneration system 4 includes a fourth discharge pipeline 405 and a catalyst regeneration reactor 401, one end of the fourth discharge pipeline 405 is connected with the bottom end of the first discharge pipeline 210, and the other end of the fourth discharge pipeline 405 is connected with the catalyst regeneration reactor 401, so that the waste catalyst is discharged into the catalyst regeneration reactor 401, the fourth discharge pipeline 405 is inclined at an angle, which facilitates the waste catalyst to slide into the catalyst regeneration reactor 401, the catalyst regeneration reactor 401 is used for removing the carbon deposit on the waste catalyst to generate regenerated catalyst, and the catalyst regeneration reactor 401 is connected with the hydrogenation reactor 201, so that the regenerated catalyst is discharged into the hydrogenation reactor 201.

[0063] Specifically, as shown in FIG. 1, the catalyst regeneration reactor 401 is provided with a regenerated gas-solid mixed flow outlet 402, a waste catalyst inlet 403 and a second gas inlet 404, the other end of the fourth discharge pipeline 405 is connected with the waste catalyst inlet 403, so that the waste catalyst enters into the catalyst regeneration reactor 401, the regenerated gas-solid mixed flow outlet 402 is used for discharging the regenerated catalyst mixed with hot air, and the second gas inlet 404 is used for introducing air.

[0064] Specifically, as shown in FIG. 1, the catalyst regeneration reactor 401 is provided with a regenerated gas-solid mixed flow outlet 402, a waste catalyst inlet 403 and a second gas inlet 404, the other end of the fourth discharge pipeline 405 is connected with the waste catalyst inlet 403, so that the waste catalyst enters into the catalyst regeneration reactor 401, the regenerated gas-solid mixed flow outlet 402 is used for discharging the regenerated catalyst mixed with hot air, and the second gas inlet 404 is used for introducing air.

[0065] In the embodiment, as shown in FIG. 1, the cyclone separation system 5 is further included, the cyclone separation system 5 is arranged between the catalyst regeneration reactor 401 and the hydrogenation reactor 201, and the cyclone separation system 5 is used for separating the regenerated catalyst and the hot air.

[0066] Specifically, as shown in FIG. 1, the cyclone separation system 5 includes a cyclone separator 501, the cyclone separation system 5 includes the 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 for separating the hot air mixed in the regenerated catalyst to dry the regenerated catalyst, the cyclone separator 501 generates a first part of the regenerated catalyst and a second part of the regenerated catalyst, the catalyst regeneration reactor 401 is provided with a gas-solid mixed flow outlet, the gas-solid mixed flow inlet 503 is connected with the gas-solid mixed flow outlet through a fifth discharge pipeline 406, so that the regenerated catalyst enters into the cyclone separator 501, the hot air outlet 502 is used for discharging the hot air, the first regenerated catalyst outlet 504 is connected with the regenerated catalyst inlet 203 arranged on the hydrogenation reactor 201 through a sixth discharge pipeline 407, so that the first part of the regenerated catalyst enters into the hydrogenation reactor 201, and the first regenerated catalyst outlet 504 is used for discharging the second part of the regenerated catalyst.

[0067] In this embodiment, the sixth discharge pipeline 407 is a heat preservation pipeline to ensure that the sixth discharge pipeline 407 insulates the first part of the regenerated catalyst.

[0068] In this embodiment, as shown in FIG. 1, a three-way valve 505 is further included, an exhaust port is arranged at the bottom of the cyclone separator 501, a first outlet of the three-way valve 505 is connected with the exhaust port, a second outlet of the three-way valve 505 is taken as a first regenerated catalyst outlet 504 to discharge the first part of the regenerated catalyst, a third outlet of the three-way valve 505 is taken as a second regenerated catalyst outlet 506 to discharge the second part of the regenerated catalyst, and the time and flow of the first part of the regenerated catalyst and the second part of the regenerated catalyst can be determined through engineering effects.

[0069] In this embodiment, the liquid condensed product and the uncondensed gas are both effective products, the pyrolysis carbon can be used to prepare carbon materials including but not limited to carbon fertilizer, activated carbon, carbon electrode carbon, etc., the liquid condensed product includes but is not limited to one or more of aromatic hydrocarbon, paraffin, olefin according to different uses of the catalyst, and the uncondensed gas is mainly CO2, CO and a small amount of low-carbon hydrocarbon, which can be used for gas fuel or chemical raw material in the future.

[0070] In this embodiment, the catalyst regeneration reactor 401 is a riser structure, air is introduced to carry out combustion reaction and carry particles to rise into the cyclone separation system 5, the carbon deposition on the waste catalyst is eliminated through combustion, and most of the heat generated by combustion is carried by the hot catalyst particles into the hydrogenation reactor 201 to maintain the hydrogenation reaction temperature.

[0071] In this embodiment, the catalyst added into the catalyst inlet is a nickel-molybdenum oxide catalyst with granular titanium oxide as a carrier.

[0072] In this embodiment, the temperature of the online catalytic hydrogenation deoxidization in the hydrogenation reactor 201 is 300-600℃, and the heat is supplied by the heat generated by the combustion of the catalyst regeneration reactor 401 and carried by the regenerated catalyst.

[0073] In summary, the present application uses the plasma torch 207 to excite hydrogen to generate high-energy active hydrogen plasma, realizes hydrogenation deoxidization of biomass pyrolysis gas in the gas phase, solves the problems of long process, large loss and high energy consumption in the process of preparing liquid fuel through high-pressure hydrogenation system to realize hydrogenation deoxidization after the biomass pyrolysis gas is condensed into bio-oil in the traditional process. Meanwhile, the online reaction is easy to control, is convenient for realizing multi-reaction integration, and is easy to design a compact reactor.

[0074] The application can realize the utilization efficiency of the catalyst through the reactor structure design, wherein the lower part of the hydrogenation reactor 201 adopts a conical or pyramid structure with an inclined angle, which can realize the rolling and sinking of the catalyst in the reactor, thereby relieving the problem of catalyst carbon deposition and deactivation. The catalyst regeneration reactor 401 adopts a riser structure, which can realize the elimination of 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 used in the hydrogenation reactor 201.

[0075] The application can realize secondary or multiple hydrogenation by recycling part of the hydrogenation products back to the hydrogenation reactor 201, and can perform the recycling hydrogenation reaction on the first incompletely reacted pyrolysis gas, thereby improving the overall conversion rate. In addition, the catalyst is recycled and regenerated by the riser combustion method, which can reduce the amount of catalyst imported and added, thereby improving the overall process economy.

[0076] The application realizes the self-supply of heat for the entire process without external heat supply by the self-supply of heat for the biomass pyrolysis reactor 101 and the supply of heat for the hydrogenation reactor 201 in the catalyst regeneration process. The plasma torch 207 used in the application can not only be powered by the power grid, but also be driven by renewable energy power such as wind power, photovoltaic power, and hydropower, thereby realizing the instant and local consumption of renewable energy power, solving the instability of renewable energy power, and further realizing the clean and low-carbon of the overall process.

[0077] The application can obtain pyrolysis carbon, liquid fuel, and three-phase products containing carbon non-condensed gas through the conversion method of biomass pyrolysis and online hydrogenation upgrading of pyrolysis gas. Through the design of the catalyst and the adjustment of the process parameters, the co-production of multiple types of target products or the directional preparation of a certain type of product can be realized, thereby realizing the resource utilization and high-value utilization of biomass.

[0078] Example 2

[0079] Example 2 provides a plasma-coupled thermal catalytic biomass gas phase online hydrogenation method, as shown in FIGS. 4 and 5, which is applied to the above-mentioned plasma-coupled thermal catalytic biomass gas phase online hydrogenation system and includes the following steps:

[0080] S1: Biomass pyrolysis: input the dry biomass raw material and dry carrier gas into the pyrolysis reactor 101, realize the biomass pyrolysis and the self-supply of heat by the bottom ignition and the control of the air volume, and make the biomass pyrolysis produce pyrolysis gas and pyrolysis carbon;

[0081] S2: Pyrolysis gas online hydrogenation: the pyrolysis gas from the pyrolysis gas outlet 105 passes through the pyrolysis gas discharge pipeline 216 and enters the hydrogenation reactant from the hydrogenation reactant inlet 209, the catalyst enters the hydrogenation reactor 201 from the catalyst inlet 202, the hydrogen plasma is generated by the hydrogen plasma generator, the pyrolysis gas is catalytically hydrogenated and deoxidized in the hydrogenation reactor 201 by the hydrogen plasma and the catalyst to generate hydrogenation products and waste catalyst, and the hydrogenation product outlet 205 is used to discharge the hydrogenation products;

[0082] S3: Product condensation separation: the hydrogenation products are discharged from the hydrogenation product outlet 205 and enter the condensation tank 301 through the hydrogenation product inlet 302, the condensation tank 301 is used to condense the hydrogenation products to obtain condensed liquid products and non-condensed gas, the condensed liquid products are discharged through the condensed liquid product outlet 304, and the non-condensed gas is discharged through the non-condensed gas outlet 303.

[0083] In this embodiment, when the hydrogenation needs to be recycled, step S4: product recycling hydrogenation is further included: a first part of the hydrogenation products discharged from the hydrogenation product outlet 205 enters the condensation tank 301 through the second discharge pipeline 214 from the hydrogenation product inlet 302, and a second part of the hydrogenation products is pumped back to the hydrogenation reactant inlet 209 by the compression pump 213 arranged on the third discharge pipeline 215, and then enters the hydrogenation reactor 201 again to perform step S2.

[0084] In this embodiment, when the catalyst regeneration system 4 is provided, step S5: catalyst recycling regeneration is further included: the waste catalyst enters the catalyst regeneration reactor 401 from the waste catalyst inlet 403 through the first discharge pipeline 210 and the fourth discharge pipeline 405, the air enters the catalyst regeneration reactor 401 from the second gas inlet 404, the combustion reaction occurs between the waste catalyst particles and the air, the carbon deposit on the waste catalyst is removed, the gas-solid mixture enters the cyclone separator 501 from the regenerated gas-solid mixture outlet 402 to realize gas-solid separation, 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 pipeline 407 to perform step S2.

[0085] In summary, the embodiment further discloses a plasma-coupled thermal catalytic biomass gas phase online hydrogenation method, which generates high-energy active hydrogen plasma by a plasma torch 207 driven by renewable energy power, and combines the heat-assisted catalytic biomass pyrolysis gas online hydrogenation generated in the catalyst regeneration process to realize low-carbon high-value conversion of biomass under the driving of renewable energy.

[0086] Obviously, many modifications and variations of the present application are possible in light of the above teachings. It is, therefore, to be understood that within the scope of the appended claims and their equivalents, the application can be practiced otherwise than as specifically described.

Claims

1. A plasma coupled thermal catalytic biomass gas phase on-line hydrogenation system, characterized in that, It comprises: a pyrolysis reaction system, comprising a pyrolysis reactor and a pyrolysis gas outlet provided on the pyrolysis reactor, the pyrolysis reactor being used for pyrolysis reaction of biomass to produce pyrolysis gas, the pyrolysis gas being discharged through the pyrolysis gas outlet; an online hydrogenation system, comprising a hydrogenation reactor, the hydrogenation reactor being provided with a hydrogenation reactant inlet, a catalyst inlet, a hydrogen plasma generator and a hydrogenation product outlet, the hydrogenation reactant inlet being connected with the pyrolysis gas outlet through a pyrolysis gas discharge pipeline, the catalyst inlet being used for adding catalyst, the hydrogen plasma generator being used for generating hydrogen plasma, the hydrogenation reactor being used for online catalytic hydrogenation and deoxidation of the pyrolysis gas through the hydrogen plasma and the catalyst to generate hydrogenation product and waste catalyst, the hydrogenation product outlet being used for discharging the hydrogenation product; a condensation system, comprising a condensation tank, the condensation tank being provided with a hydrogenation product inlet, a condensed liquid product outlet and a non-condensed gas outlet, the hydrogenation product inlet being communicated with the hydrogenation product outlet, the condensation tank being used for condensing the hydrogenation product to obtain condensed liquid product and non-condensed gas, the condensed liquid product outlet being used for discharging the condensed liquid product, and the non-condensed gas outlet being used for discharging the non-condensed gas.

2. The plasma-coupled thermal catalytic biomass gas phase online hydrogenation system according to claim 1, wherein the hydrogen plasma generator is a plasma torch, the plasma torch being provided with a hydrogen inlet and a plasma jet, the hydrogen inlet being used for introducing hydrogen, and the plasma jet being arranged at the top of the hydrogenation reactor, the plasma torch being used for ionizing hydrogen to generate hydrogen plasma, and the hydrogen plasma entering the hydrogenation reactor through the plasma jet.

3. The plasma-coupled thermal catalytic biomass gas phase online hydrogenation system according to claim 1, wherein the hydrogenation reactor is provided with a conical cavity at the lower part.

4. The plasma-coupled thermal catalytic biomass gas phase online hydrogenation system according to claim 1, further comprising a first discharge pipeline, the top end of the first discharge pipeline being communicated with the bottom of the hydrogenation reactor, the side of the first discharge pipeline being provided with a hydrogenation product outlet, and the bottom end of the first discharge pipeline being provided with a waste catalyst outlet.

5. The plasma-coupled thermal catalytic biomass gas phase online hydrogenation system according to claim 4, further comprising a second discharge pipeline and a third discharge pipeline, the hydrogenation product being divided into a first part and a second part, one end of the second discharge pipeline being connected with the hydrogenation product outlet, the other end of the second discharge pipeline being connected with the hydrogenation product inlet, so that the first part of the hydrogenation product is discharged into the condensation tank, the second discharge pipeline being provided with a circulating gas outlet, the pyrolysis gas discharge pipeline being provided with a circulating gas inlet, one end of the third discharge pipeline being connected with the circulating gas outlet, and the other end of the third discharge pipeline being connected with the circulating gas inlet, so that the second part of the hydrogenation product enters the hydrogenation reactor for cyclic hydrogenation. ​ ​ ​ ​ 6. The plasma coupled thermal catalytic biomass gas phase online hydrogenation system of claim 5, wherein: a compression pump is provided on the third discharge pipe, and the compression pump is used to extract the second part of the hydrogenation product.

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

8. The plasma coupled thermal catalytic biomass gas phase online hydrogenation system of claim 4, wherein: a catalyst regeneration system is further included, the catalyst regeneration system 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 the carbon deposit on the spent catalyst to generate regenerated catalyst, and the catalyst regeneration reactor is connected to the hydrogenation reactor to discharge the regenerated catalyst into the hydrogenation reactor.

9. The plasma coupled thermal catalytic biomass gas phase online hydrogenation system of claim 8, wherein: a cyclone separation system is further included, the cyclone separation system 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 mixed hot air in the regenerated catalyst to 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 by a fifth pipe to make the regenerated catalyst enter the cyclone separator, the hot air outlet is used to discharge the hot air, the first regenerated catalyst outlet is connected to the hydrogenation reactor by a sixth discharge pipe to make the first part of the regenerated catalyst enter the hydrogenation reactor, and the second regenerated catalyst outlet is used to discharge the first part of the regenerated catalyst.

10. A method for plasma coupled thermal catalytic biomass gas phase on-line hydrogenation, characterized by, including the following steps: biomass pyrolysis: dry biomass raw materials and dry carrier gas are input into the pyrolysis reactor, biomass pyrolysis and heat self-supply are realized by bottom ignition and control of air volume, biomass pyrolysis generates pyrolysis gas and pyrolysis carbon, and the pyrolysis gas is discharged from the pyrolysis gas outlet; online hydrogenation of pyrolysis gas: the pyrolysis gas enters the hydrogenation reactant from the hydrogenation reactant inlet through the pyrolysis gas discharge pipe, the catalyst is added into the hydrogenation reactor from the catalyst inlet, the hydrogen plasma generator generates hydrogen plasma, the pyrolysis gas is catalytically hydrogenated and deoxidized online in the hydrogenation reactor by the hydrogen plasma and the catalyst to generate hydrogenation product and spent catalyst, and the hydrogenation product outlet is used to discharge the hydrogenation product; The hydrogenated product is condensed and separated in the condensing tank, and the condensed liquid product is discharged through the condensed liquid product outlet, and the non-condensed gas is discharged through the non-condensed gas outlet.

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