WO2019029599A1 - Mobile platform-based micro biomass synthetic oil method and system - Google Patents

Abstract

A mobile platform-based micro biomass synthetic oil method and system, the method comprising integrating on a mobile platform a biomass raw material gasification unit, a synthetic gas purification conversion unit, and a Fischer-Tropsch synthesis unit that are connected in sequence and, after the mobile platform is flexibly transported according to requirements to a biomass distribution site or a set handling site, directly implementing a process for producing synthetic oil on the mobile platform. The system comprises a biomass raw material gasification unit used for gasification of biomass, a synthetic gas purification conversion unit used for purification and conversion of crude synthetic gas, and a Fischer-Tropsch synthesis unit used for implementing Fischer-Tropsch synthesis on the purified and converted synthetic gas all integrated onto a mobile platform. This system can be moved by means of being mounted on a mobile platform, and production activity is implemented thereupon, having the advantages of being on a micro scale, movable, economically feasible, flexible, and convenient.

Description

Micro-biomass synthetic oil method and system based on mobile platform Technical field

The invention relates to a biomass synthetic oil system, in particular to a method and system for miniaturizing biomass-based synthetic oil based on a mobile platform.

Background technique

With the decreasing of traditional fossil energy sources and the increasing degree of environmental pollution, the development of renewable and environmentally friendly energy sources has received increasing attention from human society. Among them, as an important renewable and environmentally friendly energy source, biomass can not only make important contributions to improving the world's primary energy structure and reducing the demand for fossil energy, but also reduce greenhouse gas emissions, ensure energy supply security, and improve trade. It plays a role in balancing, promoting rural development and improving urban waste disposal methods.

Biomass Synthetic Oil Technology (BTL) is one of the most promising biomass energy conversion technologies. Biomass can be converted to liquid fuels through biomass pretreatment, biomass gasification, syngas purification conversion, Fischer-Tropsch synthesis, and optional wax oil processing. Among them, the pretreatment process of biomass is to process the biomass raw materials through crushing, drying and molding, so that the water content and particle size of the raw materials reach the requirements of the feed of the gasifier. The gasification process of biomass is a series of high-temperature pyrolysis, oxidation, reduction and reforming reactions of biomass under certain thermodynamic conditions with the aid of a suitable gasifying agent (oxygen or water vapor) to obtain CO and The crude syngas is dominated by H ₂ and is accompanied by CH ₄ , CO ₂ , tar and residue. Biomass gasification can be divided into fixed bed gasification, moving bed gasification, fluidized bed gasification and entrained flow gasification. The purification process of syngas is to remove impurities such as sulfur, nitrogen, oxygen, chlorine and the like in the raw syngas, and adjust the ratio of H ₂ /CO in the syngas to meet the subsequent Fischer-Tropsch synthesis catalyst. And reactor requirements. The Fischer-Tropsch synthesis process converts syngas into synthetic oil (crude naphtha, heavy oil) and crude wax product under certain conditions of temperature and pressure and catalyst. Conventional Fischer-Tropsch reactors have fixed bed reactors, fluidized bed reactors and slurry bed reactors, the catalysts of which are mainly cobalt-based catalysts and iron-based catalysts. In the optional wax oil processing process, the synthetic oil can be further refined through hydrocracking, hydrorefining and fractionation processes to obtain products such as gasoline, diesel, aviation kerosene, wax and lubricating oil.

Biomass raw materials have the characteristics of low energy density, complex composition, seasonality and regionality, which bring certain difficulties to the utilization of biomass resources. The cost of collecting and transporting biomass resources is accelerating as the radius of collection increases. Therefore, large-scale bio-based synthetic oil plants have significant challenges and challenges in the collection, storage and supply of biomass materials.

According to the existence of an economical and reasonable collection radius between biomass resources and raw material collection and transportation costs, biomass resources can be divided into large collection radius biomass resources, medium collection radius biomass resources and small collection radius biomass. Resources. Among them, the large collection radius biomass resources can be supplied to a 100,000-ton BTL plant with a collection radius of 80-150 km and an annual output of 200-400,000 tons of synthetic oil; the medium-diameter biomass resources can be supplied to a 10,000-ton BTL plant. The collection radius is 30-80 km, and the annual output is 10,000-20,000 tons of synthetic oil. The small collection radius biomass resources can be supplied to the 1,000-ton BTL plant with a collection radius of 3-10 km and an annual output of 0.6-2 kg. oil.

For the remote rural areas, such as mountainous areas or forest areas, biomass resources are small collection radius biomass resources, which can meet the production needs of thousands of tons of BTL plants. Limited by the underdeveloped transportation conditions, the harsh natural environment, unstable political factors and human ecology in these areas, on the one hand, local biomass resources are not effectively utilized, and on the other hand, fuel oil products lacking in these areas need Obtained from the outside, and the transportation cost is high and the price is high.

Therefore, there is a need for a miniaturized, mobile production, more economically viable, flexible and convenient, low investment risk method and device to achieve processing and utilization of small collection radius biomass resources in remote areas, effectively reducing biomass The collection cost, while meeting the needs of local synthetic oil products.

Summary of the invention

The object of the present invention is to provide a compact, efficient, flexible and convenient mobile platform-based miniaturized biomass synthetic oil method and system.

In order to achieve the above object, the mobile platform-based miniaturized biomass synthetic oil method is a biomass material gasification unit, a syngas purification conversion unit and a Fischer-Tropsch synthesis unit which are sequentially arranged and arranged on a mobile platform. After the mobile platform is flexibly transported to the biomass distribution site or the set treatment site as needed, the process of synthetic oil production is directly performed on the mobile platform.

Preferably, the process specifically includes the following steps:

1) The biomass raw material having the particle size and the water content satisfying the feeding requirements is sent to the gasification furnace of the biomass raw material gasification unit, and the gas is reacted with air and/or oxygen as a gasifying agent to obtain a crude synthesis gas. In the decoking tank sent to the biomass feed gasification unit, the tar in the crude syngas is catalytically cracked into a small molecule gaseous substance by the decoking catalyst in the decoking tank, and then cooled and filtered to obtain a preliminary purified syngas;

2) The preliminary purified synthesis gas is sent to the conversion tank of the synthesis gas purification conversion unit, and the conversion reaction is carried out under the catalysis of the water gas shift catalyst to increase the H ₂ /CO ratio; and then sent to the purification tank of the synthesis gas purification conversion unit, By purifying different kinds of degreasers layered in the purification tank, the harmful gas impurities of various properties are removed, and the purified synthesis gas is obtained;

3) The purified synthesis synthesis gas is sent to the Fischer-Tropsch synthesis reactor of the Fischer-Tropsch synthesis unit, and the Fischer-Tropsch synthesis reaction is carried out under the catalysis of the Fischer-Tropsch catalyst, and the reaction product is separated to obtain gas oil, crude naphtha and light hydrocarbon tail gas. In order to achieve local production of small batches of biomass synthetic oil. The Fischer-Tropsch synthesis reactor adopts a microchannel reactor or a tubular fixed-bed reactor for enhancing heat and mass transfer; wherein the tubular fixed-bed reactor is preferably enhanced by internal members (such as inner fins) in the tube process. Heat transfer mass tubular fixed bed reactor. The microchannel reactor has great advantages in enhancing heat and mass transfer. For the strong exothermic Fischer-Tropsch synthesis reaction, precise temperature control during the Fischer-Tropsch synthesis process can be realized, thereby further increasing the conversion rate of the reactants and the selection of the product. Sexually, the reaction rate is greatly improved, which overcomes the disadvantages of poor heat transfer in the fixed bed reactor, the inability to use a small particle size catalyst, and the problem of the liquid phase mass transfer resistance of the slurry bed reactor and the separation of the catalyst and the product. The tube-and-tube fixed-bed reactor with internal components in the tube process enhances the heat transfer capacity of the channel by increasing the heat transfer contact point between the reaction channel and the tube wall. The tubular reactor also has simple processing and manufacturing. The catalyst is easy to load and convenient to operate. The internal component is used to enhance heat and mass transfer, so that the reactor can appropriately increase the inner diameter of the reaction pipe and shorten the length of the reactor. The above two Fischer-Tropsch synthesis reactors ensure that the reactor size is reduced and the reactor is miniaturized under a certain production intensity, so that it is more suitable for being arranged on mobile platforms such as vehicles and ships.

Preferably, in step 1), the gasification furnace has an operating temperature of 800 to 1300 ° C, an operating pressure of 0.08 to 3 MPa, and the gasifying agent is an oxygen-enriched air having an oxygen content of 25 to 50% by weight, and oxygen required. The PSA oxygen generation mechanism is obtained; the decoking catalyst is one or more of a nickel-based catalyst, charcoal, and dolomite, the decoking tank has an operating temperature of 750-900 ° C, and the tar cracking efficiency is 90-99. %; after heat removal, the heat transfer oil heat exchanger is used for heat exchange and temperature reduction; the temperature of the preliminary purified synthesis gas is 200-400 ° C, the tar content is below 5 mg/Nm ³ , and the particulate matter content is below 5 mg/Nm ³ .

Preferably, in step 2), the operating pressure of the shift tank is 1 to 3 MPa, the operating temperature is 200 to 400 ° C, and the water gas shift catalyst is a cobalt-molybdenum type water gas shift catalyst; The volume ratio of H ₂ /CO is 1.5 to 2.2, the volume content of oxygen is 5 ppm or less, and the volume content of sulfur and chlorine is 0.1 ppm or less. The Co-Mo type shift catalyst is a wide temperature sulfur-tolerant shift catalyst, and the active temperature range is 180-500 ° C. The catalyst has many advantages: 1) sulfur resistance, avoiding the cold and heat disease after the first desulfurization, and the crude synthesis of gasification The amount of water vapor in the gas can meet the requirements of the conversion, without additional steam content; 2) with organic sulfur hydroconversion function, can effectively reduce the content of organic sulfur in the shift gas; 3) high CO conversion activity, especially low temperature activity It is much higher than Fe-Cr catalyst, which can reduce the catalyst loading and reduce the reactor volume. 4) It is suitable for the catalytic conversion of crude syngas with high sulfur content in raw materials, and has the minimum requirement for sulfur in crude syngas. The upper limit is required, so the subsequent purification process is simpler; 5) the catalyst exhibits higher strength. The carrier of the cobalt-molybdenum wide temperature sulfur-tolerant shift catalyst is usually γ-Al ₂ O ₃ , magnesium-aluminum composite oxide or fine-grained spinel, and thus exhibits high strength, and the strength of the catalyst after vulcanization treatment can be improved. About 30% to 50%, in general, the strength of the iron-chromium-based shift catalyst after reduction is lower than that of the oxidation state; 6) the service life of the catalyst is relatively long.

Preferably, in step 3), the Fischer-Tropsch synthesis reactor employs a cobalt-based or iron-based catalyst, or a bifunctional catalyst having both cracking effects; the Fischer-Tropsch synthesis reactor is operated at a temperature of 200 to 350 ° C, and is operated. The pressure is 1-3 MPa, the heat transfer coefficient is 0.5-0.8 W/cm ² /K; the separation of the Fischer-Tropsch synthesis reaction product includes: I) the crude synthetic oil mixture, the waste water and the light hydrocarbon tail gas are separated by at least one-stage cooling, II The crude synthetic oil mixture is further subjected to fractional distillation to obtain gas oil and crude naphtha. The cobalt-based catalyst is a common Fischer-Tropsch synthesis catalyst, which has high Fischer-Tropsch activity and carbon chain growth ability, and has few oxygen compounds in the product, is stable during the reaction, is not easy to deposit carbon and poison, but The methane selectivity is obviously increased during the reaction at high temperature, so it can only work under low temperature conditions and is not sensitive to the water gas shift reaction. The feed gas is required to be close to the metering ratio (H ₂ /CO=2). The iron-based catalyst is also a common Fischer-Tropsch synthesis catalyst, and the reaction conditions are more adaptable. The iron-based catalyst can synthesize low-carbon olefins, heavy hydrocarbons and oxygenates with high selectivity by adjusting the auxiliary component composition or reaction temperature. Organic compounds, etc. The iron-based catalyst has a high activity for water gas shift, and the Fischer-Tropsch reaction can be carried out at a lower H ₂ /CO. The bifunctional catalyst having both cracking action is a catalyst which combines a molecular sieve or a noble metal-loaded molecular sieve with a Fischer-Tropsch synthesis catalyst. The bifunctional catalysts with cracking mainly carry out two kinds of reactions, one is the traditional Fischer-Tropsch synthesis reaction for producing hydrocarbon products, and the other is the hydrogenation of hydrocarbon products formed by Fischer-Tropsch synthesis under acid catalysis. Pyrolysis, hydroisomerization and other reactions. According to the combination method, there are mainly three kinds of bifunctional catalysts: one is a physical mixed catalyst, that is, the Fischer-Tropsch synthesis catalyst is mechanically mixed with a solid acid or a solid acid catalyst supporting a noble metal in a certain ratio; the second is a core-shell catalyst, which is at a fee. The active component of the catalyst is deposited on the surface of the solid acid membrane; the third is a supported catalyst, and the active component of the Fischer-Tropsch synthesis catalyst is directly loaded onto the solid acid. In view of the excellent acid catalysis function and spatial selection characteristics, molecular sieves are excellent carriers for one-step liquid fuel catalysts for syngas.

Preferably, in step 3), the separation of the Fischer-Tropsch synthesis reaction product is carried out by two-stage cooling separation, and the first-stage cooling separation is carried out in a thermal separation tank, the operating temperature is 120-180 ° C, the operating pressure is 1-3 MPa, and the separation is performed. The heavy oil, waste water and light hydrocarbon components are discharged; the second stage cooling separation is carried out in a cold separation tank, the operating temperature is 20-40 ° C, the operating pressure is 0.2-3 MPa, and the light hydrocarbon component of the first stage cooling separation is cold. The separation tank is cooled to separate waste water, light oil and light hydrocarbon tail gas.

Preferably, the mobile platform is further integrated with a wax oil processing unit connected to the Fischer-Tropsch synthesis unit; in the step 3), the separation of the reaction product further includes separation of the wax oil, and the separated wax oil is fed. Hydrocracking is carried out in a hydrocracking tank of a wax oil processing unit, and the required hydrogen is supplied by a PSA hydrogen generator of a wax processing unit; the operating temperature of the hydrocracking tank is 300 to 400 ° C, and the operating pressure is 6 ～ 10MPa, hydrogen oil volume ratio is 800 ~ 1500 (hydrogen oil volume ratio refers to the ratio of working hydrogen in the standard state (1atm, 0 ° C) volume flow rate and feedstock oil volume flow rate), volumetric space velocity is 0.5 ~ 2.0h ^-1 ; The hydrocracked product is fractionated to obtain gas oil and crude naphtha.

Preferably, in the step 1), if the biomass raw material does not meet the feed requirement of the biomass feedstock gasification unit, the biomass pretreatment unit pair is disposed on the mobile platform and connected to the biomass feedstock gasification unit. The biomass raw material is pretreated, that is, the particle diameter of the biomass raw material is controlled to be less than 5 cm by one or more methods of crushing, drying and molding, and the moisture content is controlled to be 25 wt% or less.

Preferably, the removing agent comprises a deoxidizing agent, a dechlorinating agent, a desulfurizing agent, and the removal order is oxygen, chlorine, sulfur; the deoxidizing agent is a copper-based catalyst (3093 deoxidizing agent) supported by activated carbon; The dechlorination agent is a catalyst containing an alkali metal or an alkaline earth metal as an active component, or a transition metal (such as Cu, Zn, Ca, Fe, Mn, etc.) which is easily combined with chlorine as an active component; the desulfurizing agent is Zinc oxide remover. The oxygen content of the syngas must be strictly controlled below 5 ppm to meet the feed requirements of the Fischer-Tropsch reaction process. Excessive oxygen content will not only cause safety problems, but also cause poisoning of subsequent catalyst deactivation. Chlorine not only poisons the catalyst surface, but also penetrates into the inner layer of the catalyst. During the desulfurization process of the synthesis gas, chlorine reacts with the desulfurizer zinc oxide. Zinc chloride is formed, and the melting point of zinc chloride is low. In the process of use, the desulfurizing agent is easily sintered to block the pores of the desulfurizing agent, which directly affects the desulfurization effect. In addition, chlorine corrodes pipes and equipment, which seriously affects the normal operation of production equipment. The sulfur-containing compound is an impurity gas which is very harmful in the synthesis gas, and easily reacts with the active metal in the Fischer-Tropsch synthesis catalyst to form a metal sulfide having no catalytic activity, causing catalyst poisoning to be deactivated.

Preferably, in step 3), the light hydrocarbon tail gas is partially or completely sent to a generator set integrated on the mobile platform for power generation for system power supply; if there is surplus, the remaining part of light hydrocarbon tail gas is recycled back to the fee. The synthesis reactor continues to participate in the synthesis reaction, or recycles back to the gasifier to continue to participate in the gasification reaction, so that the light hydrocarbon tail gas is fully utilized, the utilization of biomass resources is improved, and the emission of organic pollutants is reduced.

The invention also provides a mobile platform-based miniaturized biomass-based synthetic oil system (Mobility Biomass To Liquid, MBTL for short), which is moved by a mobile platform and performs production activities thereon, and the mobile platform is integrally arranged a biomass feedstock gasification unit, a synthesis gas purification conversion unit, and a Fischer-Tropsch synthesis unit; the biomass feedstock gasification unit includes a gasification furnace for biomass gasification, and a gas for inputting biomass raw materials to the gasification furnace Pulp furnace feeding device, PSA oxygen generator (PSA refers to pressure swing adsorption) which supplies gasification agent for gasification furnace, decoking tank for removing tar in gasification-generated crude syngas, used for heat exchange and cooling a heat transfer oil heat exchanger, a filter for filtering solid particulate matter, and a gas storage tank for buffering preliminary purification of the synthesis gas; the gasification agent inlet of the gasification furnace is connected to a gasification agent outlet of the PSA oxygen generator a synthesis gas outlet of the gasification furnace is connected to a synthesis gas inlet of the decoking tank, and a synthesis gas outlet of the decoking tank is connected to a synthesis gas inlet of the heat transfer oil heat exchanger, the heat transfer oil heat exchanger Syngas outlet and a syngas inlet of the filter is connected, the syngas outlet of the filter is connected to the syngas syngas inlet; the syngas purification conversion unit comprises a compressor for increasing syngas pressure, for increasing H ₂ /CO a shift tank and a purge tank for removing harmful impurities; the syngas inlet of the compressor is connected to a syngas outlet of the gas tank; the syngas outlet of the compressor is connected to the syngas inlet of the shift tank, The synthesis gas outlet of the conversion tank is connected to the synthesis gas inlet of the purification tank; the Fischer-Tropsch synthesis unit comprises a Fischer-Tropsch synthesis reactor, a thermal separation tank and a cold separation tank for successively cooling and separating the Fischer-Tropsch synthesis products, a fractionation column for fractionating the crude synthetic oil mixture obtained by cooling separation, and a crude naphtha tank and a gas oil tank for storing the separated oil; a syngas inlet and a purification tank for the Fischer-Tropsch synthesis reactor The synthesis gas outlet is connected, the oil and gas outlet of the Fischer-Tropsch synthesis reactor is connected to the oil and gas inlet of the thermal separation tank; the gas phase outlet of the thermal separation tank is connected to the gas phase inlet of the cold separation tank, The heavy oil outlet of the hot separation tank and the light oil outlet of the cold separation tank are respectively connected to the crude synthetic oil inlet of the fractionation column; the naphtha distillation outlet of the fractionation column is connected to the crude naphtha tank, and the fractionation tower is connected The diesel oil outlet is connected to the gas oil tank; the decoking tank is a dry decoking tank using catalytic cracking and decoking; the heat transfer oil heat exchanger is an indirect heat exchanger using heat transfer oil as a heat exchange medium; The purification tank adopts a composite high-efficiency integrated tank, and a deoxidizer layer, a dechlorination agent layer and a desulfurizer layer are sequentially disposed in the air flow direction; the Fischer-Tropsch synthesis reactor is a microchannel reactor, or a column for enhancing heat and mass transfer a tubular fixed bed reactor; the mobile platform is further integrated with a generator set configured to generate electricity by using light hydrocarbon tail gas, and the light hydrocarbon tail gas outlets of the cold separation tank and the fractionation tower are merged by a light hydrocarbon tail gas pipeline and The gas inlets of the generator set are connected.

Preferably, the light hydrocarbon tail gas line is also connected to a gasification agent inlet of the gasification furnace and a synthesis gas inlet of a Fischer-Tropsch synthesis reactor, respectively.

Preferably, the mobile platform is further integrated with a wax oil processing unit, and the wax oil processing unit comprises a wax separation tank for separating the crude wax in the Fischer-Tropsch synthesis product, and is used for hydrogenating the separated crude wax. a cracking tank, and a PSA hydrogen producing machine (PSA refers to pressure swing adsorption) for supplying hydrogen to the hydrocracking process; the wax separating tank is disposed between the oil and gas outlet of the Fischer-Tropsch synthesis reactor and the oil and gas inlet of the thermal separation tank The crude wax outlet of the wax separation tank is connected to the crude wax inlet of the hydrocracking tank; the light hydrocarbon tail gas inlet of the PSA hydrogen generator is connected to the light hydrocarbon tail gas line, and the hydrogen of the PSA hydrogen generator The outlet is connected to a hydrogen inlet of the hydrocracking tank; the cracking product outlet of the hydrocracking tank is connected to the crude synthetic oil inlet of the fractionating column.

Preferably, the mobile platform is further integrated with a biomass pretreatment unit, the biomass pretreatment unit comprises a sequentially connected crusher, a dryer and a molding machine; the gasifier feeding device comprises a lock bucket And a screw conveyor, the biomass outlet of the lock bucket is connected to the biomass inlet of the gasifier, the biomass inlet of the lock bucket is connected to the biomass outlet of the screw conveyor; the life of the screw conveyor The material inlet is connected to the biomass outlet of the molding machine.

The following is a description of the selection criteria for some devices:

1PSA oxygen generator

The large-scale commercial plant adopts an air separation device to obtain a large amount of oxygen. The air separation device is bulky and complicated in process, and the oxygen is produced through the processes of air compression, purification, refrigeration and cryogenic rectification, and is not applicable to MBTL. MBTL is preferably a PSA oxygen generator, and the smaller volume meets the oxygen supply requirements of a small gasifier, and is suitable for MBTL.

For the same reason, the hydrogen production unit selects the PSA hydrogen generator.

2 decoking tank

Large-scale commercial plants use wet spray, which requires a large amount of water. The tar content in biomass gasification synthesis gas is relatively high. It is difficult to meet the requirements of wet spray to remove tar. It is not suitable for MBTL; MBTL is dry-processed. The coke, the volume of the reactor is greatly reduced, and the MBTL can be applied.

3 heat transfer oil heat exchanger

Large-scale commercial plants use water chilling to achieve the cooling of syngas, which requires a large amount of water; MBTL prefers heat-conducting oil as the heat exchange medium, and the smaller oil consumption can meet the heat exchange requirements through recycling.

4 purification tank

Large-scale commercial plants usually use solution absorption methods, such as low-temperature washing of methanol to remove gaseous impurities in the raw syngas. The amount of solution required is large, the process is complicated, and the equipment is bulky. The purification tank uses physical adsorption to remove gaseous impurities. The composite high-efficiency integrated purification tank can realize the high-efficiency removal of coarse syngas impurities by layering different degreasers in the purification tank with the same working conditions. The purifying tank is small in volume and simple in operation, and is suitable for MBTL.

5 synthesis reactor

The large-scale commercial plant adopts a slurry bed reactor or a tubular fixed-bed reactor. The volume of the reactor is huge. The reactor volume of Shell's SMDS process is Φ7m×20m, the corresponding capacity is 5800bpd; the synthesis reactor adopts microchannel. The reactor or the tubular fixed-bed reactor with enhanced mass transfer heat transfer enhances heat transfer and mass transfer through the change of the reactor configuration, and reduces the reactor volume under the premise of ensuring the yield, and is suitable for MBTL.

6 hydrocracking reactor

Large-scale commercial plants have many types of products, high requirements for products, and complicated processing of wax oil, including hydrocracking, hydrorefining, cracking heat high score, cracking cold high score, refined heat high score, fine refrigeration high score, and Processes such as stripping, atmospheric distillation, and vacuum distillation; the hydrocracking reactor can be simply hydrocracked with wax oil to obtain a simple product (crude naphtha + gas oil), which greatly simplifies the process and meets the requirements of MBTL. .

The invention aims at transforming and utilizing biomass resources in remote rural areas, and integrates biomass pretreatment, gasification, synthesis gas purification conversion, Fischer-Tropsch synthesis, etc. into mobile platforms (such as vehicles, ships, etc.) to form an MBTL system. Realize the processing and utilization of small collection radius biomass resources, while meeting the needs of local synthetic oil products. The MBTL system is innovative and optimized from equipment selection, process parameters and routes, process links, etc. to meet mobility and economic requirements.

Compared with the prior art, the advantages of the first MBTL system of the present invention are:

1) The equipment is compact and efficient. In the selection of equipment, such as PSA oxygen generator, decoking tank, heat transfer oil heat exchanger, purification integrated tank, synthetic reactor, etc., the size of the equipment is reduced while ensuring the production scale, making the MBTL process more efficient. .

2) Environmentally friendly. The light hydrocarbon tail gas is used for power generation or partial circulation to participate in gasification or synthesis reaction, which reduces the emission of gaseous pollutants; the produced synthetic wastewater is stored in the waste water tank for unified treatment; the generated gasification waste residue is collected and used for soil fertilization.

3) Ability to achieve self-sufficiency in energy. In addition to the vehicle engine power required during system startup, the system's stable operation phase enables energy self-supply.

4) Flexible, convenient and adaptable. The invention can process different types of biomass. When the mobile platform adopts a vehicle, the vehicle can be driven on a road in a remote rural area, and self-powering can be realized during the operation of the system, so that the development of biomass resources in remote rural areas can be well applied. And use.

5) Strong economy. The cost of biomass feedstocks in remote rural areas is low, and the synthetic oil products required are limited by the traffic environment, which is difficult to transport and expensive. The invention realizes the local material, the local production, the local sales, has strong economy, and conforms to the national policy and social development direction.

6) It can be promoted. The devices involved in the invention all adopt modular design, are convenient for production, installation, and can be quickly copied, and have broad application prospects.

7) The investment risk is small. The invention has small investment, short construction period, low operating cost and greatly reduced investment risk.

DRAWINGS

FIG. 1 is a schematic diagram of the overall structure of a miniaturized biomass-based synthetic oil system based on a mobile platform provided by the present invention, wherein the pre-processing unit and the wax oil processing unit are optional parts.

2 and FIG. 3 are process flow diagrams of a miniaturized biomass-based synthetic oil system based on a mobile platform provided by the present invention. FIG. 2 includes a wax oil processing unit, and FIG. 3 does not include a wax oil processing unit.

4 is a three-dimensional perspective view of the apparatus arrangement of Embodiment 1, and the connections between the devices are reasonably set according to the process flow chart.

Figure 5 is a three-dimensional perspective view of the apparatus arrangement of Embodiment 4, and the connections between the devices are reasonably set according to the process flow chart.

Figure 6 is a schematic view showing the structure of the purification tank of Figure 2.

Wherein: the front end 100, the pretreatment unit 101, the biomass material gasification unit 102, the syngas purification conversion unit 103, the Fischer-Tropsch synthesis unit 104, the wax oil processing unit 105, the container 106, the crusher 1, the dryer 2, the molding machine 3. Screw conveyor 4, lock bucket 5, gasifier 6, PSA oxygen generator 7, decoking tank 8, heat transfer oil heat exchanger 9, filter 10, gas tank 11, compressor 12, change tank 13 , purification tank 14, deoxidizer layer 14.1, dechlorination agent layer 14.2, desulfurizer layer 14.3, Fischer-Tropsch synthesis reactor 15, hot separation tank 16, cold separation tank 17, fractionation tower 18, waste water tank 19, crude naphtha Tank 20, gas oil tank 21, wax separation tank 22, hydrocracking tank 23, PSA hydrogen generator 24

Detailed ways

The invention will be further described in detail below with reference to the drawings and specific embodiments.

As shown in FIG. 1 , the mobile platform-based miniaturized biomass synthetic oil system provided by the present invention uses a mobile platform such as a vehicle or a ship to carry and operate. Taking the vehicle platform as an example, the vehicle includes a front 100 with a generator and an engine, a frame with a loading function, and at least one container 106 for arranging the installation of the MBTL system. A pre-processing unit 101, a biomass feed gasification unit 102, a syngas purification conversion unit 103, a Fischer-Tropsch synthesis unit 104, an optional wax oil processing unit 105, and an optional generator set are integrally disposed within the container 106. 2, FIG. 3 is a process flow diagram of the MBTL system, wherein FIG. 2 includes a wax oil processing unit, FIG. 3 does not include a wax oil processing unit, and a dashed box indicates an optional device or device.

The shape, weight and transportation of transport vehicles are in compliance with the relevant laws and regulations of national road transport. The generator in the front 100 can supply electrical energy for the start of the MBTL system. The container 106 is a 40-foot high cabinet with a size of 11.8m × 2.13m × 2.72m and a gross weight of 22t and a volume of 68m ³ . The three side cabinet doors of the container can be opened for easy operation before the production operation of the device. The MBTL system covers an area of 12 to 100 m ² and carries a height of 1 to 3 m and is transported by a loading vehicle or multiple loading vehicles. When multiple loading vehicles are used, the production operation of the system is achieved by splicing.

The biomass feedstock gasification unit 102 includes a gasification furnace 6 for biomass gasification, a gasifier feed device for inputting biomass feedstock to the gasification furnace 6, and a PSA for supplying a gasification agent to the gasification furnace 6. An oxygen generator 7, a decoking tank 8 for removing tar in the gasification-generated raw syngas, a heat transfer oil heat exchanger 9 for heat exchange and temperature reduction, a filter 10 for filtering solid particles, and A gas storage tank 11 for initially purifying the synthesis gas is buffered. The gasification agent inlet of the gasification furnace 6 is connected to the gasification agent outlet of the PSA oxygen generator 7, and the synthesis gas outlet of the gasification furnace 6 is connected to the synthesis gas inlet of the decoking tank 8, and the synthesis gas outlet of the decoking tank 8 is The synthesis gas inlet of the heat transfer oil heat exchanger 9 is connected, and the synthesis gas outlet of the heat transfer oil heat exchanger 9 is connected to the synthesis gas inlet of the filter 10, and the synthesis gas outlet of the filter 10 is connected to the synthesis gas inlet of the gas storage tank 11. The gasifier feeding device comprises a lock bucket 5 and a screw conveyor 4, and the biomass outlet of the lock bucket 5 is connected with the biomass inlet of the gasifier 6, the biomass inlet of the lock bucket 5 and the biomass outlet of the screw conveyor 4. Connected.

The syngas purification conversion unit 103 includes a compressor 12 for increasing the pressure of the syngas, a shift tank 13 for increasing the H ₂ /CO ratio, and a purge tank 14 for removing harmful impurities. The syngas inlet of the compressor 12 is connected to the syngas outlet of the gas tank 11. The syngas outlet of the compressor 12 is connected to the syngas inlet of the shift tank 13, and the syngas outlet of the shift tank 13 is connected to the syngas inlet of the purge tank 14.

The Fischer-Tropsch synthesis unit 104 includes a Fischer-Tropsch synthesis reactor 15, a thermal separation tank 16 for successively cooling and separating Fischer-Tropsch synthesis products, a cold separation tank 17, and a fractionation for fractionating the crude synthetic oil mixture obtained by cooling separation. Tower 18, and a crude naphtha tank 20 and a gas oil tank 21 for storing the separated oil. The syngas inlet of the Fischer-Tropsch synthesis reactor 15 is connected to the syngas outlet of the purification tank 14, and the oil and gas outlet of the Fischer-Tropsch synthesis reactor 15 is connected to the oil and gas inlet of the thermal separation tank 16. The gas phase outlet of the hot separation tank 16 is connected to the gas phase inlet of the cold separation tank 17, and the heavy oil outlet of the hot separation tank 16 and the light oil outlet of the cold separation tank 17 are connected to the crude synthetic oil inlet of the fractionation column 18, respectively. The naphtha distillation outlet of the fractionation column 18 is connected to the crude naphtha tank 20, and the diesel outlet of the fractionation column 18 is connected to the gas oil tank 21.

The decoking tank 8 is a dry decoking tank using catalytic cracking and decoking. The heat transfer oil heat exchanger 9 is an indirect heat exchanger in which a heat transfer oil is used as a heat exchange medium.

As shown in Fig. 6, the purification tank 14 is a composite high-efficiency integrated tank in which a deoxidizer layer 14.1, a dechlorination agent layer 14.2 and a desulfurizer layer 14.3 are sequentially disposed in the gas flow direction. The Fischer-Tropsch synthesis reactor 15 is a microchannel reactor, or a tubular fixed bed reactor that enhances heat and mass transfer.

The biomass pretreatment unit 101 comprises a crusher 1, a dryer 2 and a forming machine 3 which are connected in series, and the biomass outlet of the molding machine 3 is connected to the biomass inlet of the screw conveyor 4. If the biomass feedstock itself meets the feed requirements, the biomass pretreatment unit 101 may not be provided.

The light hydrocarbon tail gas outlets of the cold separation tank 17 and the fractionation column 18 are connected to the gas inlet of the generator set through the light hydrocarbon tail gas line. The light hydrocarbon tail gas line is also connected to the gasification agent inlet of the gasification furnace 6, and the synthesis gas inlet of the Fischer-Tropsch synthesis reactor 15, respectively.

The wax oil processing unit 105 includes a wax separation tank 22 for separating the crude wax in the Fischer-Tropsch synthesis product, a hydrocracking tank 23 for cracking the separated crude wax, and a hydrogenation of PSA for supplying hydrogen for the hydrocracking process. Machine 24. The wax separation tank 22 is disposed between the oil and gas outlet of the Fischer-Tropsch synthesis reactor 15 and the oil and gas inlet of the thermal separation tank 16, and the crude wax outlet of the wax separation tank 22 is connected to the crude wax inlet of the hydrocracking tank 23. The light hydrocarbon tail gas inlet of the PSA hydrogen generator 24 is connected to a light hydrocarbon tail gas line, and the hydrogen outlet of the PSA hydrogen generator 24 is connected to the hydrogen inlet of the hydrocracking tank 23. The cracked product outlet of the hydrocracking tank 23 is connected to the crude synthetic oil inlet of the fractionation column. If the Fischer-Tropsch synthesis uses a bifunctional catalyst having both cracking action, the wax oil processing unit 105 may not be provided.

The production process of the MBTL system will be described in detail below.

The collected biomass feedstock first enters the biomass pretreatment unit 101. In the biomass pretreatment unit 101, the biomass raw material is crushed by the crusher 1 to a particle size of 0 to 5 cm; and dried by a dryer 2 to have a moisture content of 0 to 25 wt%; finally, it is extruded through a molding machine 3 to make The particle size of the biomass reaches 0 to 5 cm. The biomass pretreatment unit has a processing capacity of 5 to 150 tpd (tons per day) of biomass. After pretreatment by the biomass pretreatment unit 101, the biomass feedstock can meet the feed requirements of the biomass feedstock gasification unit 102.

The biomass pellet obtained by the pretreatment of the biomass material enters the lock bucket 5 through the screw conveyor 4, and the pressure of the lock bucket 5 can reach 0.2 to 3 MPa, and then enters the gasifier 6. The gasification furnace 6 is a horizontal fixed bed gasification furnace or a vertical fixed bed gasification furnace, and the operating temperature is 800 to 1300 ° C, and the operating pressure is 0.08 to 3 MPa. The gasifying agent is air, oxygen-enriched or oxygen. When oxygen or oxygen is used, the PSA oxygen generator 7 is used to supply oxygen to the gasifier. The crude syngas from the gasifier is removed by the decoking tank 8 to remove potential tar, the catalytic decoking temperature is 750-900 ° C, the catalytic decoking efficiency is 90-99%, and then cooled by the heat transfer oil heat exchanger 9 (after heating The heat transfer oil is sent to the external air cooling device or the water cooling device for cooling), the temperature is lowered to 200-400 ° C, the solid impurities are removed through the filter 10, the tar content is 0-5 mg/Nm ³ , and the particulate matter content is 0-5 mg/Nm. ³ . The resulting preliminary purified syngas enters the gas storage tank 11 for temporary storage. The gasification furnace 6 has a gasification intensity of 300 to 1000 kg/m ² /h, a treatment capacity of 5 to 150 tpd of biomass, and a gas generating capacity of 3,000 to 90,000 Nm ³ /d. Using a higher temperature of 800-1300 ° C, a higher pressure of 0.08 ~ 3MPa, the gasification intensity can be controlled at 300 ~ 1000kg / m ² / h, and in this gasification intensity range, the size of the gasifier can be in the vehicle The installation in the space, and within the above temperature range, can effectively reduce the tar content, while meeting the temperature requirements of subsequent tar catalytic cracking.

The preliminary purified synthesis gas from the biomass feedstock gasification unit 102 enters the synthesis gas purification conversion unit 103. The processing capacity of the synthesis gas purification conversion unit is 3000 to 90000 Nm ³ /d, which can increase the H ₂ /CO volume ratio in the synthesis gas to 1.5 to 2.2, and the sulfur content and chlorine content are reduced to 0 to 0.1 ppm, including The amount of oxygen is reduced to 0 to 5 ppm.

The compressor 12 raises the pressure of the preliminary purification synthesis gas to 1 to 3 MPa and then enters the shift tank 13. The shift tank 13 is a cobalt-molybdenum type water gas shift catalyst having an operating temperature of 200 to 400 ° C and an operating pressure of 1 to 3 MPa, which can increase the H ₂ /CO volume ratio to 1.5 to 2.2. The converted syngas enters the purification tank 14, and the operating temperature is 200 to 400 ° C, and the operating pressure is 1 to 3 MPa. The purification tank 14 adopts a composite high-efficiency integrated purification tank, and the different degreasing agents, including a desulfurizing agent, a deoxidizing agent and a dechlorinating agent, are loaded in different tank layers, and the order of removal is oxygen, chlorine and sulfur, and the syngas can be used in the syngas. The sulfur content and chlorine content are reduced to 0-0.1ppm, the oxygen content is reduced to 0-5ppm; the deoxidizer is a copper-based catalyst supported by activated carbon; the dechlorination agent is a catalyst containing an alkali metal or an alkaline earth metal as an active component. Or a transition metal which is easily combined with chlorine is a catalyst of an active ingredient; the desulfurizing agent is a zinc oxide remover. Several degreasing agents work under the same operating conditions to achieve a removal effect.

The purge-transformed synthesis gas from the purification conversion unit 103 enters the Fischer-Tropsch synthesis unit 104. The Fischer-Tropsch synthesis reactor 15 has an operating temperature of 200 to 350 ° C and an operating pressure of 1 to 3 MPa. The heat transfer coefficient of the Fischer-Tropsch synthesis reactor is controlled at 0.5-0.8 W/cm ² /K. In the heat transfer coefficient range, the synthesis reactor can remove the heat generated by the Fischer-Tropsch synthesis reaction in time, and on the other hand, reduce the catalyst bed. The temperature of the layer hot spot increases the service life of the catalyst, and on the other hand, the overall synergistic efficiency of the reactor and the catalyst is improved, and the production capacity is enhanced, so that the demand for the vehicle production can be better met.

The Fischer-Tropsch catalyst employs a conventional cobalt- or iron-based catalyst or a bifunctional catalyst having cracking action. If a bifunctional catalyst is used, the Fischer-Tropsch synthesized product exits the Fischer-Tropsch synthesis reactor 15 (Fig. 3) and directly enters the thermal separation tank 16 to obtain heavy oil (mainly diesel components), wastewater and light hydrocarbons, respectively. Component. The thermal separation tank 16 has an operating temperature of 120 to 180 ° C and an operating pressure of 1 to 3 MPa. The wastewater enters the waste water tank 19 from the bottom of the hot separation tank 16, the heavy oil enters the fractionation column 18 from the side line, and the light hydrocarbon component enters the cold separation tank 17. The operating temperature of the cold separation tank 17 is 20 to 40 ° C, and the operating pressure is 0.2 to 3 MPa. At the bottom of the cold separation tank, the waste water enters the waste water tank 19, and the light oil (mainly the naphtha component) from the side line enters the fractionation tower 18, and the light hydrocarbon tail gas is emitted from the top. Crude naphtha and gas oil are separately obtained from the fractionation column 18, and enter the crude naphtha tank 20 and the gas oil tank 21, respectively. At least a portion of the light hydrocarbon tail gas is sent to the generator set for power generation, and the remainder is recycled back to the Fischer-Tropsch synthesis reactor 15 to continue to participate in the synthesis reaction, or recycled back to the gasifier 6 to continue to participate in the gasification reaction. The gasification waste produced by Fischer-Tropsch synthesis is collected for soil fertilization.

If a cobalt-based or iron-based catalyst is used, the Fischer-Tropsch synthesis product contains a crude wax, which is required to enter the optional wax oil processing unit 105 for wax processing (Fig. 2), specifically: first, the wax separation tank 22, The crude wax and other hydrocarbon components are separated and the other hydrocarbon components enter the thermal separation column 16. The crude wax enters the hydrocracking tank 23 to undergo a hydrocracking reaction, cracks the long-chain hydrocarbon into a short-chain hydrocarbon, and the obtained product enters the fractionating column 18. The operating temperature of the hydrocracking column is 300-400 ° C, the operating pressure is 6-10 MPa, the hydrogen-oil ratio is 800-1500, and the volumetric space velocity is 0.5-2.0 h ^-1 . The circulating hydrogen is supplied from the PSA hydrogen generator 24. The raw material of the hydrogen generator may be derived from the crude syngas of the gas storage tank 11.

The biomass processing capacity of the MBTL system is 5 to 150 tpd (ton/day), and the raw materials are agricultural and forestry wastes mainly composed of straw, twigs, sapwood, wood chips, biomass-forming fuel, processed livestock manure, And one or more of the classified household wastes. The synthetic oil has a capacity of 5 to 100 bpd (barrel/day) and the products are crude naphtha and gas oil. The yield of crude naphtha is 15% to 30% (mass fraction), the yield of gas oil is 30% to 75% (mass fraction), and the yield of tail gas is 5% to 30% (mass fraction), here The yield of a product refers to the mass fraction of each product in the total product.

The various unit devices involved above may not be limited to the biomass synthetic oil technology, and may be used alone or in combination with other processes: 1) the pretreatment unit may be separately used for biomass crushing treatment; 2) the biomass feed gasification unit may be applied. The gasification process for other applications of syngas; 3) the syngas purification conversion unit can be applied to other gas purification processes; 4) the Fischer-Tropsch synthesis unit can be applied to natural gas, flare gas, oil field gas, gas purge As a raw material Fischer-Tropsch synthesis process, the synthesis reactor can be used as a highly efficient heat exchanger without loading the catalyst; 5) The wax oil processing unit can also be used in other hydrocracking and hydrofinishing processes.

Several embodiments are given below for different application scales.

Example 1

In this embodiment, the straw is used as a biomass raw material, the treatment amount is 12 tpd, and the production capacity is 10 bpd synthetic oil. All equipment is installed in a container, and the installation is shown in Figure 4. The Fischer-Tropsch synthesis reactor 15 employs a microchannel reactor, and the Fischer-Tropsch synthesis catalyst employs a bifunctional catalyst having a cracking action. The Fischer-Tropsch synthesized oil contains no wax, so the wax oil processing unit 105 is not used. Light hydrocarbon tail gas is all used to generate electricity to power the system. The specific process parameters are shown in Table 1.

Example 2

In this embodiment, the sapwood is a biomass material, the treatment amount is 18 tpd, and the production capacity is 30 bpd synthetic oil. The Fischer-Tropsch synthesis reactor 15 employs a microchannel reactor, and the Fischer-Tropsch synthesis catalyst employs a bifunctional catalyst having a cracking action. The Fischer-Tropsch synthesized oil contains no wax, so the wax oil processing unit 105 is not used. Light hydrocarbon tail gas is all used to generate electricity to power the system. The specific process parameters are shown in Table 1.

Example 3

In this embodiment, the straw-forming fuel is used as a biomass material, the treatment amount is 45 tpd, and the production capacity is 50 bpd. The Fischer-Tropsch synthesis reactor 15 employs a tubular fixed bed reactor, the catalyst uses an iron-based catalyst, and the Fischer-Tropsch synthesized oil contains wax oil, so a wax oil processing unit 105 is required. The light hydrocarbon tail gas is recycled back to the Fischer-Tropsch synthesis reactor and the other half is used to generate electricity for the system. The specific process parameters are shown in Table 1.

Example 4

In this embodiment, a mixture of chicken manure and sapwood (mass ratio 1:1) is used as a biomass material, the treatment amount is 63 tpd, and the production capacity is 70 bpd synthetic oil. All equipment is installed in three containers, and the installation is shown in Figure 5. The Fischer-Tropsch synthesis reactor 15 uses a microchannel reactor, the Fischer-Tropsch synthesis catalyst uses a cobalt-based catalyst, and the Fischer-Tropsch synthesized oil contains a wax oil, so a wax oil processing unit 105 is required. The light hydrocarbon tail gas is recycled halfway back to the Fischer-Tropsch synthesis reactor and the other half is used to power the system. The specific process parameters are shown in Table 1.

Example 5

In this embodiment, a mixture of domestic garbage and sapwood (1:1) is used as a biomass material, and the treatment amount is 108 tpd, and the production capacity is 90 bpd synthetic oil. The Fischer-Tropsch synthesis reactor 15 employs a microchannel reactor, and the catalyst employs a cobalt-based catalyst having a cracking action. The Fischer-Tropsch synthesized oil does not contain wax, so the wax oil processing unit 105 is not used. A quarter of the light hydrocarbon tail gas is recycled back to the synthesis reactor 15, one quarter of which is recycled back to the gasifier 6, and the remaining one is used to generate electricity to power the system. The specific process parameters are shown in Table 1.

Table 1 Process parameters of each embodiment

Claims (13)

A method for miniaturizing biomass-based synthetic oil based on mobile platform, characterized in that: it is a biomass material gasification unit (102), a syngas purification conversion unit (103) and a fee which are sequentially connected and arranged on a mobile platform. The mixing unit (104) performs the process of synthetic oil production directly on the mobile platform after the mobile platform is flexibly transported to the biomass distribution site or the set processing site as needed. The mobile platform-based miniaturized biomass synthetic oil method according to claim 1, wherein the process comprises the following steps: 1) The biomass raw material having the particle size and the moisture satisfying the feeding requirement is sent to the gasification furnace (6) of the biomass raw material gasification unit (102), and is gasified with air and/or oxygen as a gasifying agent. The obtained crude syngas is sent to the decoking tank (8) of the biomass feedstock gasification unit (102), and the tar in the crude syngas is catalytically cracked into a small molecular gas state by the decoking catalyst in the decoking tank (8). The substance is further cooled and filtered to obtain a preliminary purification synthesis gas; 2) The preliminary purified synthesis gas is sent to the conversion tank (13) of the synthesis gas purification conversion unit (103), and the conversion reaction is carried out under the catalytic action of the water gas shift catalyst to increase the H ₂ /CO ratio; and then the synthesis gas purification conversion is carried out. In the purification tank (14) of the unit (103), different kinds of decontaminants which are layered and filled in the purification tank (14) are used to remove harmful gas impurities of various properties to obtain a purified conversion synthesis gas; 3) The purified synthesis synthesis gas is sent to the Fischer-Tropsch synthesis reactor (15) of the Fischer-Tropsch synthesis unit (104), and the Fischer-Tropsch synthesis reactor (15) adopts a microchannel reactor or a tube-and-tube type that enhances heat and mass transfer. The fixed bed reactor is subjected to Fischer-Tropsch synthesis under the catalysis of Fischer-Tropsch catalyst, and the reaction product is separated to obtain gas oil, crude naphtha and light hydrocarbon tail gas, thereby realizing local production of small batch biomass synthetic oil. The mobile platform-based miniaturized biomass synthetic oil method according to claim 2, wherein in the step 1), the gasification furnace (6) has an operating temperature of 800 to 1300 ° C and an operating pressure of 0.08 to 3 MPa. The gasifying agent is oxygen-enriched air having an oxygen content of 25 to 50% by weight, and the required oxygen is obtained by using a PSA oxygen generator (7); the decoking catalyst is one of a nickel-based catalyst, charcoal, and dolomite. Or a plurality of, the operating temperature of the decoking tank (8) is 750-900 ° C, the tar cracking efficiency is 90-99%; after the de-focusing, the heat transfer oil heat exchanger (9) is used for heat exchange cooling; The temperature for purifying the synthesis gas is 200 to 400 ° C, the tar content is 5 mg/Nm ³ or less, and the particulate matter content is 5 mg/Nm ³ or less. The method for miniaturizing biomass-based synthetic oil based on mobile platform according to claim 2, wherein in the step 2), the operating pressure of the conversion tank (13) is 1 to 3 MPa, and the operating temperature is 200 ～. 400 ° C, the water gas shift catalyst is a cobalt-molybdenum type water gas shift catalyst; in the purification conversion synthesis gas, the H ₂ /CO volume ratio is 1.5 to 2.2, the volume content of oxygen is below 5 ppm, and the volume content of sulfur and chlorine is Below 0.1 ppm. The mobile platform-based miniaturized biomass synthetic oil method according to claim 2, wherein in the step 3), the Fischer-Tropsch synthesis reactor (15) adopts a cobalt-based or iron-based catalyst, or both a bifunctional catalyst having a cracking effect; the Fischer-Tropsch synthesis reactor has an operating temperature of 200 to 350 ° C, an operating pressure of 1 to 3 MPa, a heat transfer coefficient of 0.5 to 0.8 W/cm ² /K; and a Fischer-Tropsch synthesis reaction product The separation comprises: I) separating the crude synthetic oil mixture, waste water and light hydrocarbon tail gas by at least one stage of cooling, II) the crude synthetic oil mixture and then fractionating to obtain gas oil and crude naphtha. The mobile platform-based miniaturized biomass synthetic oil method according to claim 2, wherein the mobile platform is further integrated with a wax oil processing unit (105) connected to the Fischer-Tropsch synthesis unit (104); In the step 3), the separation of the reaction product further comprises separation of the wax oil, and the separated wax oil is sent to the hydrocracking tank (23) of the wax oil processing unit (105) for hydrocracking, hydrogen required. Provided by a PSA hydrogen generator (24) of a wax oil processing unit (105); the hydrocracking tank (23) has an operating temperature of 300 to 400 ° C, an operating pressure of 6 to 10 MPa, and a hydrogen oil volume ratio of 800 ～. 1500, the volumetric space velocity is 0.5 to 2.0 h ^-1 ; the hydrocracked product is fractionated to obtain gas oil and crude naphtha. The mobile platform-based miniaturized biomass synthetic oil method according to claim 2, wherein in the step 1), if the biomass raw material does not satisfy the feed requirement of the biomass feedstock gasification unit (102), The biomass feedstock is pretreated by integrating the biomass pretreatment unit (101) disposed on the mobile platform and connected to the biomass feed gasification unit (102), by one or more of crushing, drying and forming. In the manner, the particle diameter of the biomass raw material is controlled to be 5 cm or less, and the moisture content is controlled to be 25 wt% or less. The method for miniaturizing biomass-based synthetic oil based on mobile platform according to claim 2, wherein the removing agent comprises a deoxidizing agent, a dechlorinating agent and a desulfurizing agent, and the order of removal is oxygen, chlorine and sulfur; The deoxidizing agent is a copper-based catalyst supported on activated carbon; the dechlorinating agent is a catalyst having an alkali metal or an alkaline earth metal as an active component, or a transition metal which is easily combined with chlorine as an active component; The desulfurizing agent is a zinc oxide removing agent. The method for miniaturizing biomass-based synthetic oil based on mobile platform according to any one of claims 2 to 8, wherein in the step 3), part or all of the light hydrocarbon tail gas is integrated into the moving arrangement. The generator set on the platform generates electricity for system energy supply; if there is surplus, the remaining part of the light hydrocarbon tail gas is recycled back to the Fischer-Tropsch synthesis reactor (15) to continue to participate in the synthesis reaction, or to recycle back to the gasifier (6) to continue Participate in the gasification reaction. A miniaturized biomass-based synthetic oil system based on a mobile platform, which is moved by a mobile platform and performs production activities thereon, wherein the mobile platform is integrally arranged with a biomass material gasification unit (102), a synthesis gas purification conversion unit (103) and a Fischer-Tropsch synthesis unit (104); The biomass feedstock gasification unit (102) includes a gasifier (6) for biomass gasification, a gasifier feed device for inputting biomass feedstock to the gasifier (6), and gasification The furnace (6) provides a PSA oxygen generator (7) for gasifying agent, a decoking tank (8) for removing tar from the crude syngas formed by gasification, and a heat transfer oil heat exchanger for heat exchange and cooling ( 9) a filter (10) for filtering solid particulate matter, and a gas storage tank (11) for buffering preliminary purification of synthesis gas; a gasification agent inlet of the gasification furnace (6) and a PSA oxygen generator ( 7) The gasification agent outlet is connected, the synthesis gas outlet of the gasification furnace (6) is connected to the synthesis gas inlet of the decoking tank (8), the synthesis gas outlet of the decoking tank (8) and the heat conduction The synthesis gas inlet of the oil heat exchanger (9) is connected, the synthesis gas outlet of the heat transfer oil heat exchanger (9) is connected to the synthesis gas inlet of the filter (10), and the synthesis gas outlet of the filter (10) Connected to the synthesis gas inlet of the gas storage tank (11); The syngas purification conversion unit (103) includes a compressor (12) for increasing the pressure of the syngas, a shift tank (13) for increasing the H ₂ /CO ratio, and a purification tank for removing harmful impurities (14). The synthesis gas inlet of the compressor (12) is connected to the synthesis gas outlet of the gas storage tank (11); the synthesis gas outlet of the compressor (12) is connected to the synthesis gas inlet of the conversion tank (13). The syngas outlet of the shift tank (13) is connected to the syngas inlet of the purification tank (14); The Fischer-Tropsch synthesis unit (104) comprises a Fischer-Tropsch synthesis reactor (15), a thermal separation tank (16) for successively cooling and separating Fischer-Tropsch synthesis products, and a cold separation tank (17) for separating the cooling. a fractionation column (18) for fractionating the obtained crude synthetic oil mixture, and a crude naphtha tank (20) for storing the separated oil and a gas oil canister (21); the Fischer-Tropsch synthesis reactor (15) a synthesis gas inlet connected to the synthesis gas outlet of the purification tank (14), the oil and gas outlet of the Fischer-Tropsch synthesis reactor (15) being connected to the oil and gas inlet of the thermal separation tank (16); the thermal separation tank (16) The gas phase outlet is connected to the gas phase inlet of the cold separation tank (17), and the heavy oil outlet of the hot separation tank (16) and the light oil outlet of the cold separation tank (17) are respectively connected to the crude synthetic oil inlet of the fractionation column (18); The naphtha distillation outlet of the fractionation column (18) is connected to a crude naphtha tank (20), and the diesel outlet of the fractionation column (18) is connected to the gas oil tank (21); The decoking tank (8) is a dry decoking tank using catalytic cracking and decoking; the heat transfer oil heat exchanger (9) is an indirect heat exchanger using heat transfer oil as a heat exchange medium; (14) A composite high-efficiency integrated tank is provided, which is provided with a deoxidizer layer (14.1), a dechlorination agent layer (14.2) and a desulfurizer layer (14.3) in this order along the gas flow direction; the Fischer-Tropsch synthesis reactor (15) is a microchannel reactor, or a tubular fixed bed reactor for enhanced heat and mass transfer; The mobile platform is further integrated with a generator set arranged to generate electricity by using light hydrocarbon tail gas, and the light hydrocarbon tail gas outlets of the cold separation tank (17) and the fractionation tower (18) are merged by the light hydrocarbon tail gas pipeline and the power generation The gas inlets of the unit are connected. The mobile platform-based miniaturized biomass synthesis oil system according to claim 10, wherein the light hydrocarbon tail gas pipeline is further connected to the gasification agent inlet of the gasification furnace (6), Fischer-Tropsch The synthesis gas inlet of the synthesis reactor (15) is connected. The mobile platform-based miniaturized biomass synthetic oil system according to claim 10 or 11, wherein the mobile platform is further integrated with a wax oil processing unit (105), and the wax oil processing unit ( 105) comprising a wax separation tank (22) for separating the crude wax in the Fischer-Tropsch synthesis product, a hydrocracking tank (23) for cracking the separated crude wax, and a hydrogenation PSA for supplying hydrogen to the hydrocracking process. The wax separation tank (22) is disposed between the oil and gas outlet of the Fischer-Tropsch synthesis reactor (15) and the oil and gas inlet of the thermal separation tank (16), and the wax separation tank (22) The crude wax outlet is connected to the crude wax inlet of the hydrocracking tank (23); the light hydrocarbon tail gas inlet of the PSA hydrogen generator (24) is connected to the light hydrocarbon tail gas line, the PSA hydrogen generator (24) The hydrogen outlet is connected to the hydrogen inlet of the hydrocracking tank (23); the cracking product outlet of the hydrocracking tank (23) is connected to the crude synthetic oil inlet of the fractionating column. The mobile platform-based miniaturized biomass synthetic oil system according to claim 10 or 11, wherein the mobile platform is further integrated with a biomass pretreatment unit (101), and the biomass pretreatment The unit (101) comprises a sequentially connected crusher (1), a dryer (2) and a forming machine (3); the gasifier feeding device comprises a lock bucket (5) and a screw conveyor (4), The biomass outlet of the lock bucket (5) is connected to the biomass inlet of the gasifier (6), and the biomass inlet of the lock bucket (5) is connected to the biomass outlet of the screw conveyor (4); The biomass inlet of the screw conveyor (4) is connected to the biomass outlet of the forming machine (3).

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