Biomass processing and utilizing system and method

Abstract

The invention discloses a biomass processing and utilizing system and method. The biomass processing and utilizing system comprises a gasification-thermal conversion integrated reactor, a biomass hydrogen production reactor, a purification reactor and an oxidation regeneration reactor, wherein the gasification-thermal conversion integrated reactor comprises a gasification area and a thermal conversion area, and the gasification area and the thermal conversion area are of an integrated structure. The invention further provides a biomass processing and utilizing method adopting the system. A new method is provided for efficient processing and utilization of biomass by exerting the resource attributes of the biomass, the defect that the resource utilization rate of a traditional biomass gasification technology is low is overcome, the biomass serves as a carbon source, and cyclic utilization of carbon resources is achieved through organic coupling of a hydrogen and heat combined supply system.

Description

Technical Field

[0001] The present invention belongs to the technical field of biomass treatment, and in particular relates to a biomass processing and utilization system and method. Background Art

[0002] Biomass is a renewable energy source and also a renewable carbon source. At present, the annual output of major biomass in my country is about 3.49 billion tons. The development potential of biomass as energy is about 460 million tons of standard coal. The current utilization is only 60 million tons of standard coal. The potential for biomass utilization in the future is huge. Therefore, promoting the utilization of biomass resources is an important task for energy conservation and emission reduction, which meets the current demand for green and low-carbon development. Among them, biomass gasification is an important research direction.

[0003] Biomass gasification is a process that uses biomass as raw material, oxygen (air, oxygen-rich gas or pure oxygen), water vapor, hydrogen, etc. as gasifying agents, and converts biomass into combustible gas through thermochemical reactions under high temperature conditions. Biomass gasification technology can convert low-grade solid biomass into high-grade combustible gas. The combustible gas obtained after biomass gasification generally contains components such as carbon monoxide, carbon dioxide, and hydrogen. At present, the combustible gas obtained after biomass gasification is generally used for heating and power generation. From the perspective of carbon cycle, it is only used for heating and power generation, which only utilizes the energy properties of biomass and fails to bring into play the resource properties of biomass. The dilemma of biomass gasification is mainly that the gasification products are not utilized as resources, and the benefits are not outstanding.

[0004] According to the composition analysis of combustible gas, it will have great advantages if the carbon dioxide in the combustible gas is removed and converted. The components of the combustible gas after decarbonization are carbon monoxide and hydrogen. After adjusting the hydrogen-carbon ratio, it can be further converted into chemical products through synthesis gas, thus realizing the carbon cycle.

[0005] Therefore, studying the effective ways to utilize biomass materials and energy is related to the development prospects of biomass resource utilization. Summary of the invention

[0006] In view of the shortcomings of the prior art, the present invention provides a biomass processing and utilization system and method. By giving full play to the resource attributes of biomass, a new method is proposed for the efficient processing and utilization of biomass, overcoming the shortcomings of low resource utilization rate of traditional biomass gasification technology, using biomass as a carbon source, and realizing the recycling of carbon resources through the organic coupling of hydrogen and heat cogeneration systems.

[0007] The first aspect of the present invention provides a biomass processing and utilization system, including a gasification-thermal conversion integrated reactor, a biomass hydrogen production reactor, a purification reactor and an oxidation regeneration reactor; wherein:

[0008] The gasification-heat conversion integrated reactor comprises a gasification zone and a heat conversion zone, and the gasification zone and the heat conversion zone are an integrated structure; the heat conversion zone comprises a first straight tube section and a contraction section from top to bottom, and the gasification zone comprises an expansion section and a second straight tube section from top to bottom, and the contraction section of the heat conversion zone and the expansion section of the gasification zone form a sleeve structure; a riser is arranged inside the heat conversion zone, and the top port of the riser is located in the first straight tube section of the heat conversion zone; the bottom port of the riser passes through the bottom of the shell of the second straight tube section of the gasification zone; the gasification zone is provided with a feed inlet, a gas phase outlet, and a solid phase outlet; the heat conversion zone is provided with a gas phase outlet and a solid phase outlet;

[0009] The hydrogen production reactor is provided with a water vapor inlet, a gas phase outlet, a solid phase inlet and a solid phase outlet; the oxidation regeneration reactor is provided with a feed inlet and a discharge port; the purification reactor is provided with a gas phase feed inlet, a solid phase feed inlet, a gas phase outlet and a solid phase outlet;

[0010] Among them, the solid phase outlet of the gasification zone of the gasification-thermal conversion integrated reactor is connected with the solid phase inlet of the hydrogen production reactor through a pipeline; the gas phase outlet of the gasification zone is connected with the gas phase feed port of the purification reactor through a pipeline; the solid phase outlet of the hydrogen production reactor is connected with the feed port of the oxidation regeneration reactor through a pipeline, and the gas phase outlet of the hydrogen production reactor is divided into two routes, one of which is connected with the contraction section of the thermal conversion zone through a pipeline, and the other is connected with the bottom port of the riser through a pipeline, and the discharge port of the oxidation regeneration reactor is connected with the expansion section of the gasification zone through a pipeline; the solid phase outlet of the thermal conversion zone is connected with the solid phase feed port of the purification reactor through a pipeline, and the solid phase outlet of the purification reactor is connected with the bottom port of the inner tube through a pipeline.

[0011] Furthermore, in the above-mentioned biomass processing and utilization system, the heat conversion zone is provided with a riser, the interior of the riser is a first heat conversion reaction space, and the space between the riser and the heat conversion zone shell is a second heat conversion reaction space.

[0012] Furthermore, in the above-mentioned biomass processing and utilization system, the gasification zone and the heat conversion zone are coaxially arranged, and the diameters of the second straight cylinder section of the gasification zone and the first straight cylinder section of the heat conversion zone can be the same or different; the riser of the heat conversion zone vertically passes through the heat conversion zone and the gasification zone, and the bottom port of the riser extends out of the bottom of the second straight cylinder section of the gasification zone.

[0013] Furthermore, in the above-mentioned biomass processing and utilization system, the gasification zone and the heat conversion zone are an integrated structure and are not interconnected.

[0014] Furthermore, in the above-mentioned biomass processing and utilization system, a gas-solid separation device is connected to the top end of the riser in the heat conversion zone, and the gas-solid separation device can be a cyclone separator.

[0015] Furthermore, in the above-mentioned biomass processing and utilization system, a gas-solid separation device is arranged on the top of the thermal conversion zone, and the gas-solid separation device can be a cyclone separator, and further more than one level of cyclone separators can be arranged.

[0016] Furthermore, in the above-mentioned biomass processing and utilization system, a gas-solid separation device is arranged on the top of the gasification zone, and the gas-solid separation device may be a cyclone separator, and further more than one level of cyclone separators may be arranged.

[0017] Furthermore, in the above-mentioned biomass processing and utilization system, the oxidation regeneration reactor adopts a riser reactor, and the oxidation regeneration reactor is provided with a feed port and a discharge port, wherein one end of the discharge port is connected to a gas-solid separation device, and the gas-solid separation device can be a cyclone separator, and further more than one level of cyclone separators can be provided.

[0018] Furthermore, in the above-mentioned biomass processing and utilization system, the hydrogen production reactor can be any one of a fixed bed, a moving bed, and a fluidized bed reactor, preferably a fluidized bed reactor.

[0019] Furthermore, in the above-mentioned biomass processing and utilization system, a gas-solid separation device may be provided on the top of the hydrogen production reactor. The gas-solid separation device may be a cyclone separator, and further more than one level of cyclone separators may be provided.

[0020] Furthermore, in the above-mentioned biomass processing and utilization system, the purification reactor can be any one of a fixed bed, a moving bed, and a fluidized bed reactor, preferably a moving bed reactor.

[0021] Furthermore, the above-mentioned biomass processing and utilization system includes a synthesis gas conversion reactor, and the gas phase outlet of the thermal conversion zone and the gas phase outlet of the purification reactor are connected to the feed inlet of the synthesis gas conversion reactor through pipelines respectively.

[0022] Furthermore, in the above-mentioned biomass processing and utilization system, the gas phase outlet of the heat conversion zone is arranged on the top shell of the straight cylinder section, and the solid phase outlet of the heat conversion zone is arranged on the shell at the bottom of the contraction section.

[0023] Furthermore, in the above-mentioned biomass processing and utilization system, the feed inlet of the gasification zone is arranged on the shell at the top of the expansion section, the gas phase outlet of the gasification zone is arranged on the shell at the top of the expansion section, and the solid phase outlet of the gasification zone is arranged on the shell at the bottom of the second straight cylinder section.

[0024] Furthermore, in the above-mentioned biomass processing and utilization system, the gas phase inlet of the hydrogen production reactor is arranged on the shell at the top of the hydrogen production reactor, the water vapor inlet is arranged on the shell at the bottom of the hydrogen production reactor, the solid phase inlet is arranged on the shell at the top of the hydrogen production reactor, and the solid phase outlet is arranged on the shell at the bottom of the hydrogen production reactor.

[0025] Furthermore, in the above-mentioned biomass processing and utilization system, the gas phase feed port of the purification reactor is arranged at the lower part of the shell of the purification reactor, the solid phase feed port of the purification reactor is arranged at the upper part of the shell of the purification reactor, the gas phase outlet of the purification reactor is arranged at the top of the shell of the purification reactor, and the solid phase outlet of the purification reactor is arranged at the bottom of the shell of the purification reactor.

[0026] Another aspect of the present invention provides a biomass processing and utilization method, comprising the following steps:

[0027] (1) The biomass raw material enters the gasification zone of the gasification-thermal conversion integrated reactor and reacts in the presence of an auxiliary agent to obtain a first gas phase stream and a first solid phase stream. The heat released by the gasification reaction of the biomass in the gasification zone provides heat for the thermal conversion zone.

[0028] (2) The first gas phase stream obtained in step (1) is contacted with calcium oxide in a purification reactor for reaction, and a second gas phase stream and a second solid phase stream are obtained after the reaction;

[0029] (3) The first solid-phase stream obtained in step (1) and water vapor enter a hydrogen production reactor for reaction, and after the reaction, a third gas-phase stream and a third solid-phase stream are obtained;

[0030] (4) a portion of the third gas-phase stream obtained in step (3) is used as a fluidizing medium to lift the second solid-phase stream obtained in step (2) and carry it into the riser of the thermal conversion zone for reaction; after the reaction product is separated into gas and solid, the obtained solid enters the thermal conversion zone for further reaction and separation to obtain a fourth gas-phase stream and a fourth solid-phase stream; another portion of the third gas-phase stream obtained in step (3) enters the contraction section of the thermal conversion zone for reaction;

[0031] (5) The third solid-phase stream obtained in step (3) undergoes an oxidation reaction in an oxidative regeneration reactor under the action of an oxygen-containing atmosphere, and after the reaction, a fifth gas-phase stream and a fifth solid-phase stream are obtained; the fifth solid-phase stream is circulated back to the gasification zone as an auxiliary agent to react with the biomass raw material.

[0032] Furthermore, in the above-mentioned biomass processing and utilization method, the operating conditions of the gasification zone in step (1) are as follows: the reaction temperature is 500-1000°C, preferably 650-850°C; the reaction pressure is 0.1-2Mpa, preferably 0.2-1Mpa.

[0033] Furthermore, in the above-mentioned biomass processing and utilization method, the biomass raw material described in step (1) can be derived from any material containing lignocellulose, and can be one or more of corn stalks, rice husks, wheat straw, and wood chips; the biomass raw material is generally first dried and dehydrated, and the drying and dehydration treatment is preferably carried out by microwave drying, the microwave frequency is generally 2400±500MHZ, the drying time is 5-20min, and the moisture content of the biomass after dehydration is usually controlled to be 5-20wt%.

[0034] Furthermore, in the above-mentioned biomass processing and utilization method, the second gas stream obtained in step (2) and the fourth gas stream obtained in step (4) can be used as raw materials for synthesis gas conversion reaction to prepare low-carbon olefins (C2-C4), methanol and other products.

[0035] Furthermore, in the above-mentioned biomass processing and utilization method, the operating conditions of the hydrogen production reactor in step (3) are as follows: the reaction temperature is 400-1100°C, preferably 500-900°C; the reaction pressure is 0.1-2Mpa, preferably 0.2-1Mpa.

[0036] Furthermore, in the above-mentioned biomass processing and utilization method, the first gas phase feed stream includes carbon monoxide, carbon dioxide and hydrogen, and the molar ratio of carbon monoxide, carbon dioxide and hydrogen in the first gas phase feed stream can be controlled to be (0.1-10):(0.01-5):1, preferably (0.4-6):(0.1-2):1.

[0037] Furthermore, in the above-mentioned biomass processing and utilization method, the auxiliary agent in step (1) is a composite oxide containing Fe, Ce and Ni elements, and the Fe / Ce molar ratio in the composite oxide is 1:(0.01-10), preferably 1:(0.1-5); the Fe / Ni molar ratio in the composite oxide is 1:(0.1-10), preferably 1:(0.2-3).

[0038] Furthermore, in the above-mentioned biomass processing and utilization method, the mass ratio of the biomass raw material to the auxiliary agent in step (1) is 1: (10-100), preferably 1: (20-50).

[0039] Furthermore, in the above-mentioned biomass processing and utilization method, the reaction pressure in the thermal conversion zone in step (4) is 0.1-2 MPa, preferably 0.2-1 MPa.

[0040] Furthermore, in the above-mentioned biomass processing and utilization method, the third gas phase stream is used as fluidizing wind to bring the second solid phase stream (calcium carbonate) into the riser for reaction and transport it upward; the thermal conversion zone adopts the form of a fluidized bed reactor, and the calcium carbonate is completely decomposed under the action of hydrogen by extending the residence time. The fourth solid phase stream separated after the reaction is transported to the purification reactor through a pipeline for reaction.

[0041] Furthermore, in the above-mentioned biomass processing and utilization method, the third solid phase stream obtained in step (3) enters the oxidation regeneration reactor to contact with the oxygen-containing atmosphere for reaction, and the fifth solid phase stream obtained after the reaction is circulated back to the gasification zone for repeated use. The operating conditions of the oxidation regeneration reactor are as follows: the reaction temperature is 500-1200°C, preferably 700-1000°C; the reaction pressure is 0.1-2Mpa, preferably 0.2-1Mpa. The oxygen-containing atmosphere can be oxygen, air, etc.

[0042] Furthermore, in the above-mentioned biomass processing and utilization method, the biomass raw material is preferably first dried and dehydrated; microwave drying can be used, the microwave drying conditions are 2400±500MHZ, the drying time is 5-20min, and the water content of the biomass raw material after dehydration is 5-20wt%.

[0043] Compared with the prior art, the main beneficial effects of the biomass processing and utilization system and method technical solution provided by the present invention are mainly reflected in the following aspects:

[0044] 1. The present invention provides a gasification-heat conversion integrated reaction form, in which the gasification zone and the heat conversion zone are coaxially arranged, and the overall structure is compact and occupies a small area; at the same time, the gasification zone and the heat conversion zone adopt a sleeve structure design scheme, which can fully utilize the heat of the gasification zone to heat the heat conversion zone, improve the utilization efficiency of the heat in the system, and have a significant energy-saving advantage.

[0045] 2. In the biomass processing and utilization method provided by the present invention, the auxiliary agent can be recycled between the gasification zone, the hydrogen production reactor, and the oxidation regeneration reactor. First, it can promote the gasification reaction of the biomass raw material in the gasification zone. The auxiliary agent will lose lattice oxygen and convert into a reduced state during the gasification reaction. In the hydrogen production unit, it will greatly promote the water vapor hydrogen production reaction. The auxiliary agent after the reaction in the hydrogen production unit enters the oxidation unit, undergoes further oxidation reaction, and then circulates back to the gasification unit for repeated use.

[0046] 3. In the biomass processing and utilization method provided by the present invention, calcium oxide is used to react with the first gas phase stream to achieve decarbonization of the carbon-containing fuel gas. The second gas phase stream obtained after the treatment mainly consists of carbon monoxide and hydrogen, which can be converted into synthetic gas for chemical use. In addition, the calcium carbonate generated by the reaction can also significantly reduce the decomposition and conversion temperature under a hydrogen atmosphere, and convert carbon dioxide into carbon monoxide in situ. After adjusting the corresponding hydrogen-carbon ratio with hydrogen, it can also be converted into synthetic gas for chemical use. BRIEF DESCRIPTION OF THE DRAWINGS

[0047] Figure 1 It is a schematic diagram of a biomass processing and utilization system and method provided by the present invention.

[0048] 1. Biomass raw material; 2. Gasification-thermal conversion integrated reactor; 3. Gasification zone; 301. Expansion section; 302. Second straight barrel section; 4. Thermal conversion zone; 401. First straight barrel section; 402. Contraction section; 403 Riser; 5. Purification reactor; 6. Hydrogen production reactor; 7. Oxidation regeneration reactor; 8. Water vapor; 9. Oxygen-containing atmosphere; 10. Syngas conversion reactor; 11. First gas-solid separation device; 12. The second gas-solid separation device; 13, the third gas-solid separation device; 14, the fourth gas-solid separation device; 15, the fifth gas-solid separation device; 21, the first gas-phase feed stream; 22, the first solid-phase feed stream; 41, the fourth gas-phase feed stream; 42, the fourth solid-phase feed stream; 51, the second gas-phase feed stream; 52, the second solid-phase feed stream; 61, the third gas-phase feed stream; 62, the third solid-phase feed stream; 71, the fifth gas-phase feed stream; 72, the fifth solid-phase feed stream. DETAILED DESCRIPTION

[0049] The biomass processing and utilization method and system provided by the present invention are further described below in conjunction with the accompanying drawings and specific embodiments.

[0050] Unless explicitly stated otherwise, throughout the specification and claims, the term “comprise” or variations such as “include” or “comprising”, etc., will be understood to include the stated elements or components but not to exclude other elements or components.

[0051] In this document, for the convenience of description, spatial relative terms such as "below", "below", "down", "above", "above", "upper", etc. may be used to describe the relationship between one element or feature and another element or feature in the accompanying drawings. It should be understood that the spatial relative terms are intended to include different orientations of the object in use or operation in addition to the orientation depicted in the figure. For example, if the object in the figure is turned over, the element described as being "below" or "below" other elements or features will be oriented "above" the element or feature. Therefore, the exemplary term "below" can include both below and above. Objects may also have other orientations (rotated 90 degrees or other orientations) and the spatial relative terms used in this document should be interpreted accordingly.

[0052] In this document, the terms "first", "second", etc. are used to distinguish two different elements or parts, and are not used to limit a specific position or relative relationship. In other words, in some embodiments, the terms "first", "second", etc. can also be interchangeable.

[0053]

[0043] All numerical values ​​for parameters (eg, amounts or conditions) herein are to be understood as being modified in all instances by the term "about," whether or not "about" actually appears before the numerical value.

[0054] The present invention provides a biomass processing and utilization system, including a gasification-thermal conversion integrated reactor 2, a hydrogen production reactor 6, a purification reactor 5 and an oxidation regeneration reactor 7; wherein the gasification-thermal conversion integrated reactor 2 includes a gasification zone 3 and a thermal conversion zone 4, and the gasification zone 3 and the thermal conversion zone 4 are an integrated structure; the thermal conversion zone 4 includes a first straight tube section 401 and a contraction section 402 from top to bottom, and the gasification zone 3 includes an expansion section 301 and a second straight tube section 302 from top to bottom, and the contraction section 402 of the thermal conversion zone and the expansion section 301 of the gasification zone form a sleeve structure; a riser 403 is arranged inside the thermal conversion zone 4, and the top port of the riser 403 is located in the first straight tube section 401 of the thermal conversion zone; the bottom port of the riser 403 passes through the second straight tube section 302 of the gasification zone The bottom of the shell; the top end of the riser is connected to the first gas-solid separation device 11, the gasification zone 3 is provided with a feed inlet, a gas phase outlet, and a solid phase outlet; the top of the gasification zone is provided with a third gas-solid separation device 13, the thermal conversion zone 4 is provided with a gas phase outlet and a solid phase outlet, the top of the thermal conversion zone 3 is provided with a first gas-solid separation device 11 and a second gas-solid separation device 12; the hydrogen production reactor 6 is provided with a water vapor inlet, a gas phase outlet, a solid phase inlet and a solid phase outlet; the top of the hydrogen production reactor 6 is provided with a fifth gas-solid separation device 15; the oxidation regeneration reactor 7 is provided with a feed inlet and a discharge port; the top outlet of the oxidation regeneration reactor 7 is connected to the fourth gas-solid separation device 14; the purification reactor 5 is provided with a gas phase feed inlet, a solid phase feed inlet, a gas phase outlet and a solid phase outlet.

[0055] The biomass raw material 1 is first dried and dehydrated. The biomass raw material after drying and dehydration enters the gasification zone 3 of the gasification-thermal conversion integrated reactor 2, and reacts in the presence of an auxiliary agent. After the reaction, a first gas phase stream 21 and a first solid phase stream 22 are obtained; the first gas phase stream 21 is discharged through the gas phase outlet and then enters the purification reactor 5 through the gas phase feed inlet of the purification reactor 5 to contact with calcium oxide for reaction, and after the reaction, a second gas phase stream 51 and a second solid phase stream 52 are obtained; the first solid phase stream 22 is discharged through the solid phase outlet of the gasification zone 3 and enters through the solid phase inlet of the hydrogen production reactor 6, and contacts with water vapor 8 for reaction, and after the reaction, a third gas phase stream 61 and a third solid phase stream 62 are obtained; the third solid phase stream 62 is discharged through the solid phase outlet and enters the oxidation regeneration reactor 7, and an oxidation regeneration reaction is carried out in the presence of an oxygen-containing atmosphere 9, and after the reaction, a fifth gas phase stream 71 and a fifth solid phase stream 72 are obtained. Phase material flow 72, the 5th solid-phase material flow 72 (regenerated auxiliary agent) enters the gasification zone 3 to participate in the reaction; the 5th gas-phase material flow 71 is discharged from the reactor; the obtained 3rd gas-phase material flow 61 is divided into two paths, one of which is the third gas-phase material flow 61 discharged through the gas phase outlet and enters the contraction section 402 of the thermal conversion zone to participate in the reaction; the other third gas-phase material flow 61 is discharged through the gas phase outlet and used as a fluidizing medium to lift the 2nd solid-phase material flow into the lifting pipe 403 of the thermal conversion zone for reaction and is separated through the first gas-solid separation device 11 at the outlet, and the separated solid-phase material continues to react in the thermal conversion zone 4; after the reaction is completed, the 4th gas-phase material flow 41 and the 4th solid-phase material flow 42 are separated through the second gas-solid separation device 12 at the outlet, wherein the 4th gas-phase material flow 41 and the 2nd gas-phase material flow 51 are mixed and then enter the synthesis gas conversion reactor 10 for reaction; the obtained 4th solid-phase material flow 42 enters the purification reactor 5 and contacts with the 1st gas-phase material flow 21 for reaction.

[0056] Example 1

[0057] Sawdust was used as the biomass raw material, and dehydration treatment was carried out under the conditions of 2600MHZ and drying time of 20min. The moisture content of the raw material after dehydration was 6wt%. The biomass raw material after drying and dehydration treatment was added to the gasification zone of the gasification-thermal conversion integrated reactor at a rate of 100g / h, and reacted with the auxiliary agent at 662°C, wherein the Fe / Ce molar ratio of the auxiliary agent was 0.23, the Fe / Ni molar ratio was 0.60, and the solid circulation rate was 4290.33g / h. After the reaction, the first gas phase stream and the first solid phase stream were obtained; the molar ratio of carbon monoxide, carbon dioxide and hydrogen in the first gas phase stream was 2.66 / 0.396 / 1; the first gas phase stream was discharged through the gas phase outlet and then entered the purification reactor through the gas phase feed port of the purification reactor to contact with calcium oxide to react and remove CO 2, the solid feed rate of CaO is 21.16 g / h, and after the reaction, a second gas phase stream and a second solid phase stream are obtained; the first solid phase stream obtained is discharged through the solid phase outlet of the gasification zone and enters through the solid phase inlet of the hydrogen production reactor, contacts with water vapor and reacts at 584°C, and after the reaction, a third gas phase stream and a third solid phase stream are obtained; the third solid phase stream obtained is discharged through the solid phase outlet and enters the oxidation regeneration reactor, and an oxidation regeneration reaction is carried out in an atmosphere with an oxygen concentration of 3% and at 715°C, and after the reaction, a fifth gas phase stream and a fifth solid phase stream are obtained. The 5th solid-phase stream (regenerated additive) is circulated into the gasification zone to participate in the reaction; the 5th gas-phase stream is discharged from the reactor as the flue gas after regeneration; the obtained 3rd gas-phase stream is divided into two paths, one of which is discharged through the gas-phase outlet and enters the contraction section of the thermal conversion zone to participate in the reaction; the other third gas-phase stream is discharged through the gas-phase outlet and serves as the fluidizing medium to lift the 2nd solid-phase stream into the riser of the thermal conversion zone for reaction and is separated through the first gas-solid separation device at the outlet, and the separated solid-phase material continues to react in the thermal conversion zone to convert CO 2 After the reaction is completed, the 4th gas-phase material flow and the 4th solid-phase material flow are separated by the second gas-solid separation device at the outlet; the obtained 4th solid-phase material flow enters the purification reactor and contacts with the 1st gas-phase material flow for reaction. The 4th gas-phase material flow and the 2nd gas-phase material flow are mixed and then enter the synthesis gas conversion reactor to react with light olefins at 370°C and 2.4MPa. The yield of light olefins after the reaction is 440.89g / h.

[0058] Example 2

[0059] Sawdust was used as the biomass raw material, and dehydration treatment was carried out under the conditions of 2600MHZ and drying time of 20min. The moisture content of the raw material after dehydration was 6wt%. The biomass raw material after drying and dehydration treatment was added to the gasification zone of the gasification-thermal conversion integrated reactor at a rate of 100g / h, and reacted with the auxiliary agent at 825°C, wherein the Fe / Ce molar ratio of the auxiliary agent was 0.13, the Fe / Ni molar ratio was 0.47, and the solid circulation rate was 3408.73g / h. After the reaction, the first gas phase stream and the first solid phase stream were obtained; the molar ratio of carbon monoxide, carbon dioxide and hydrogen in the first gas phase stream was 1.17 / 0.09 / 1; the first gas phase stream was discharged through the gas phase outlet and then entered the purification reactor through the gas phase feed port of the purification reactor to contact with calcium oxide to react and remove CO 2, the solid feed rate of CaO is 12.54 g / h, and after the reaction, a second gas phase stream and a second solid phase stream are obtained; the first solid phase stream obtained is discharged through the solid phase outlet of the gasification zone and enters through the solid phase inlet of the hydrogen production reactor, contacts with water vapor and reacts at 816°C, and after the reaction, a third gas phase stream and a third solid phase stream are obtained; the third solid phase stream obtained is discharged through the solid phase outlet and enters the oxidation regeneration reactor, and an oxidation regeneration reaction is carried out at 938°C in an atmosphere with an oxygen concentration of 2.6%, and after the reaction, a fifth gas phase stream and a fifth solid phase stream are obtained. The 5th solid-phase stream (regenerated additive) is circulated into the gasification zone to participate in the reaction; the 5th gas-phase stream is discharged from the reactor as the flue gas after regeneration; the obtained 3rd gas-phase stream is divided into two paths, one of which is discharged through the gas-phase outlet and enters the contraction section of the thermal conversion zone to participate in the reaction; the other third gas-phase stream is discharged through the gas-phase outlet and serves as a fluidizing medium to lift the 2nd solid-phase stream into the riser of the thermal conversion zone for reaction and is separated through the first gas-solid separation device at the outlet, and the separated solid-phase material continues to react in the thermal conversion zone to convert CO 2 After the reaction is completed, the 4th gas-phase material flow and the 4th solid-phase material flow are separated by the second gas-solid separation device at the outlet; the obtained 4th solid-phase material flow enters the purification reactor to contact with the 1st gas-phase material flow for reaction. The 4th gas-phase material flow and the 2nd gas-phase material flow are mixed and then enter the synthesis gas conversion reactor to react with methanol at 240°C and 5.1MPa. The yield of the product methanol after the reaction is 104.5g / h.

[0060] Example 3

[0061] The main process is the same as that of Example 1, except that: the temperature of the gasification zone is 786°C, the auxiliary agent circulation rate is 3660.33 g / h, the auxiliary agent Fe / Ce molar ratio is 0.12, the auxiliary agent Fe / Ni molar ratio is 0.53, the molar ratio of carbon monoxide, carbon dioxide and hydrogen in the first gas phase stream is 1.35 / 0.11 / 1, the CaO solid feed rate is 12.46 g / h, the hydrogen production reactor temperature is 786°C, and the oxidation regenerator temperature is 981°C. After the reaction, the output of light olefins is 459.3 g / h.

[0062] Example 4

[0063] The main process is the same as that of Example 2, except that: the biomass raw material is straw, the temperature of the gasification zone is 804°C, the auxiliary agent circulation rate is 2687.06 g / h, the auxiliary agent Fe / Ce molar ratio is 0.72, the auxiliary agent Fe / Ni molar ratio is 0.32, the molar ratio of carbon monoxide, carbon dioxide and hydrogen in the first gas phase stream is 0.98 / 0.45 / 1, the CaO solid feed rate is 35.22 g / h, the hydrogen production reactor temperature is 748°C, and the oxidation regenerator temperature is 869°C. After the reaction, the methanol output is 69.5 g / h.

[0064] Example 5

[0065] The main process is the same as that of Example 1, except that: the biomass raw material is straw, the temperature of the gasification zone is 690°C, the auxiliary agent circulation rate is 3692.67 g / h, the auxiliary agent Fe / Ce molar ratio is 3.82, the auxiliary agent Fe / Ni molar ratio is 2.95, the molar ratio of carbon monoxide, carbon dioxide and hydrogen in the first gas phase stream is 0.46 / 1.13 / 1, the CaO solid feed rate is 89.26 g / h, the hydrogen production reactor temperature is 655°C, and the oxidation regenerator temperature is 761°C. After the reaction, the output of light olefins is 338.6 g / h.

[0066] Example 6

[0067] The main process is the same as that of Example 2, except that: the temperature of the gasification zone is 718°C, the auxiliary agent circulation rate is 4348.17 g / h, the molar ratio of the auxiliary agent Fe / Ce is 0.30, the molar ratio of the auxiliary agent Fe / Ni is 0.45, the molar ratio of carbon monoxide, carbon dioxide and hydrogen in the first gas phase stream is 5.06 / 0.95 / 1, the CaO solid feed rate is 24.28 g / h, the temperature of the hydrogen production reactor is 682°C, and the temperature of the oxidation regenerator is 798°C. After the reaction, the methanol output is 95.5 g / h.

Claims

1. A biomass processing and utilization system, comprising a gasification-thermal conversion integrated reactor, a biomass hydrogen production reactor, a purification reactor and an oxidation regeneration reactor; in, The gasification-thermal conversion integrated reactor comprises a gasification zone and a thermal conversion zone, and the gasification zone and the thermal conversion zone are an integrated structure; The heat conversion zone includes a first straight tube section and a contraction section from top to bottom, and the gasification zone includes an expansion section and a second straight tube section from top to bottom, and the contraction section of the heat conversion zone and the expansion section of the gasification zone form a sleeve structure; A riser is provided inside the heat conversion zone, and the top port of the riser is located in the first straight section of the heat conversion zone; the bottom port of the riser passes through the bottom of the second straight section shell of the gasification zone; the gasification zone is provided with a feed port, a gas phase outlet, and a solid phase outlet; The heat conversion zone is provided with a gas phase outlet and a solid phase outlet; The hydrogen production reactor is provided with a water vapor inlet, a gas phase outlet, a solid phase inlet and a solid phase outlet; the oxidation regeneration reactor is provided with a feed inlet and a discharge port; the purification reactor is provided with a gas phase feed inlet, a solid phase feed inlet, a gas phase outlet and a solid phase outlet; Among them, the solid phase outlet of the gasification zone of the gasification-thermal conversion integrated reactor is connected with the solid phase inlet of the hydrogen production reactor through a pipeline; the gas phase outlet of the gasification zone is connected with the gas phase feed port of the purification reactor through a pipeline; the solid phase outlet of the hydrogen production reactor is connected with the feed port of the oxidation regeneration reactor through a pipeline, and the gas phase outlet of the hydrogen production reactor is divided into two routes, one of which is connected with the contraction section of the thermal conversion zone through a pipeline, and the other is connected with the bottom port of the riser through a pipeline, and the discharge port of the oxidation regeneration reactor is connected with the expansion section of the gasification zone through a pipeline; the solid phase outlet of the thermal conversion zone is connected with the solid phase feed port of the purification reactor through a pipeline, and the solid phase outlet of the purification reactor is connected with the bottom port of the inner tube through a pipeline.

2. The biomass processing and utilization system according to claim 1, Features: The heat conversion zone is provided with a riser, the interior of the riser is a first heat conversion reaction space, and the space between the riser and the heat conversion zone shell is a second heat conversion reaction space.

3. The biomass processing and utilization system according to claim 1, Features: The gasification zone and the heat conversion zone are coaxially arranged, and the diameters of the second straight section of the gasification zone and the first straight section of the heat conversion zone can be the same or different; the riser of the heat conversion zone vertically passes through the heat conversion zone and the gasification zone, and the bottom port of the riser extends out of the bottom of the second straight section of the gasification zone.

4. The biomass processing and utilization system according to claim 1, Features: The gasification zone and the heat conversion zone are an integrated structure and are not interconnected.

5. The biomass processing and utilization system according to claim 1, Features: The top end of the riser in the heat conversion zone is connected with a gas-solid separation device, which is a cyclone separator.

6. The biomass processing and utilization system according to claim 1, Features: A gas-solid separation device is arranged on the top of the heat conversion zone. The gas-solid separation device is a cyclone separator, and more than one level of cyclone separators are arranged.

7. The biomass processing and utilization system according to claim 1, Features: A gas-solid separation device is arranged on the top of the gasification zone. The gas-solid separation device is a cyclone separator, and more than one level of cyclone separators are arranged.

8. The biomass processing and utilization system according to claim 1, Features: The oxidation regeneration reactor adopts a riser reactor, and the oxidation regeneration reactor is provided with a feed port and a discharge port, wherein one end of the discharge port is connected with a gas-solid separation device, and the gas-solid separation device is a cyclone separator, and more than one cyclone separator is provided.

9. The biomass processing and utilization system according to claim 1, Features: A gas-solid separation device is arranged on the top of the hydrogen production reactor. The gas-solid separation device is a cyclone separator, and more than one level of cyclone separators are arranged.

10. The biomass processing and utilization system according to claim 1, Features: The biomass processing and utilization system comprises a synthesis gas conversion reactor, and the gas phase outlet of the heat conversion zone and the gas phase outlet of the purification reactor are respectively connected with the feed port of the synthesis gas conversion reactor through pipelines.

11. A method for processing and utilizing biomass, comprising the following steps: (1) The biomass raw material enters the gasification zone of the gasification-thermal conversion integrated reactor and reacts in the presence of an auxiliary agent to obtain a first gas phase stream and a first solid phase stream. The heat released by the gasification reaction of the biomass in the gasification zone provides heat for the thermal conversion zone. (2) The first gas phase stream obtained in step (1) is contacted with calcium oxide in a purification reactor for reaction, and a second gas phase stream and a second solid phase stream are obtained after the reaction; (3) The first solid-phase stream obtained in step (1) and water vapor enter a hydrogen production reactor for reaction, and after the reaction, a third gas-phase stream and a third solid-phase stream are obtained; (4) a portion of the third gas-phase stream obtained in step (3) is used as a fluidizing medium to lift the second solid-phase stream obtained in step (2) and carry it into the riser of the thermal conversion zone for reaction; after the reaction product is separated into gas and solid, the obtained solid enters the thermal conversion zone for further reaction and separation to obtain a fourth gas-phase stream and a fourth solid-phase stream; another portion of the third gas-phase stream obtained in step (3) enters the contraction section of the thermal conversion zone for reaction; (5) The third solid-phase stream obtained in step (3) is subjected to an oxidation reaction in an oxidative regeneration reactor under the action of an oxygen-containing atmosphere to obtain a fifth gas-phase stream and a fifth solid-phase stream. The fifth solid-phase stream is circulated back to the gasification zone as an auxiliary agent to react with the biomass raw material.

12. The biomass processing and utilization method according to claim 11, Features: The operating conditions of the gasification zone in step (1) are as follows: the reaction temperature is 500-1000°C, preferably 650-850°C; the reaction pressure is 0.1-2Mpa, preferably 0.2-1Mpa.

13. The biomass processing and utilization method according to claim 11, Features: The biomass raw material in step (1) is derived from any material containing lignocellulose, and is selected from one or more of corn stalks, rice husks, wheat straw, and wood chips.

14. The biomass processing and utilization method according to claim 11, Features: The biomass raw material is dried and dehydrated, and the moisture content of the biomass after dehydration is controlled to be 5-20wt%.

15. The biomass processing and utilization method according to claim 11, Features: The operating conditions of the hydrogen production reactor in step (3) are as follows: the reaction temperature is 400-1100° C., preferably 500-900° C.; the reaction pressure is 0.1-2 MPa, preferably 0.2-1 MPa.

16. The biomass processing and utilization method according to claim 11, Features: The auxiliary agent in step (1) is a composite oxide containing Fe, Ce and Ni elements, wherein the Fe / Ce molar ratio in the composite oxide is 1:(0.01-10), preferably 1:(0.1-5); the Fe / Ni molar ratio in the composite oxide is 1:(0.1-10), preferably 1:(0.2-3).

17. The biomass processing and utilization method according to claim 11, Features: In step (1), the mass ratio of the biomass raw material to the auxiliary agent is 1:(10-100), preferably 1:(20-50).

18. The biomass processing and utilization method according to claim 11, Features: The reaction pressure in the thermal conversion zone in step (4) is 0.1-2 MPa, preferably 0.2-1 MPa.

19. The biomass processing and utilization method according to claim 11, Features: The third gas phase stream is used as fluidizing air to bring the second solid phase stream into the riser for reaction and transport it upward; the fourth solid phase stream separated after the reaction is transported to the purification reactor through a pipeline for reaction.

20. The biomass processing and utilization method according to claim 11, Features: The third solid phase stream obtained in step (3) enters the oxidation regeneration reactor to contact with the oxygen-containing atmosphere for reaction, and the fifth solid phase stream obtained after the reaction is circulated back to the gasification zone for repeated use; the operating conditions of the oxidation regeneration reactor are as follows: the reaction temperature is 500-1200°C, preferably 700-1000°C; the reaction pressure is 0.1-2Mpa, preferably 0.2-1Mpa.

Images