A method and system for producing a SAF syngas from biomass gasification based on a bubbling fluidized bed

Abstract

The present application belongs to the technical field of biomass gasification, and particularly relates to a method and system for preparing SAF synthetic gas based on a bubbling fluidized bed. The system comprises, in sequence, a bubbling fluidized bed gasifier, a cyclone separator, a hot catalytic filtration-reforming integrated device, a reconfigurable dry deep purification unit, and a water gas shift and CO2 removal and recycling unit. At least two layers of gasification agent nozzles are arranged on the axial sides of the freeboard area of the gasifier. The reconfigurable dry deep purification unit is provided with a plurality of switchable adsorption beds, and is configured with an online analysis and program control system based on synthetic gas impurity fingerprints. The water gas shift and CO2 removal and recycling unit is provided with a CO2 return pipe for conveying part of the removed CO2 to the freeboard area. The present application can long-term and stably output synthetic gas meeting the requirements of a SAF synthetic catalyst by means of a systematic strategy of tar source inhibition, purification bed sequence reconfiguration according to impurity spectrum, and ratio adjustment and heat management linkage.

Description

Technical Field

[0001] This invention belongs to the field of biomass gasification technology, specifically relating to a method and system for preparing SAF syngas based on bubbling fluidized bed biomass gasification. Background Technology

[0002] Biomass gasification-synthetic fuel (BtL) is one of the important routes for synthesizing sustainable aviation fuel (SAF), but the core challenge for its large-scale engineering application lies in the difficulty of producing clean syngas that meets the stringent requirements of downstream synthesis catalysts in a long-term, stable, and economical manner. Existing technologies have significant limitations in both gasification source control and syngas purification: First, there are shortcomings in suppressing byproducts at the gasification source. Bubbling fluidized bed gasifiers possess excellent heat transfer performance, feedstock adaptability, and operational stability. However, under typical operating temperature windows, a considerable amount of tar and light hydrocarbons as byproducts is unavoidable. More importantly, the inherent composition and moisture content fluctuations of biomass feedstocks further amplify the instability of tar and impurity yields. Studies have shown that increasing the temperature and oxidation intensity of the free plate zone through methods such as secondary injection can effectively reduce tar yield, revealing that "coordinated management of the reaction atmosphere and temperature in the free plate zone" is a crucial entry point for suppressing tar formation. However, existing gasification process designs often lack refined and proactive control strategies for this region, resulting in insufficient source suppression of tar, thus shifting the purification pressure downstream.

[0003] Secondly, downstream syngas purification systems face the dual constraints of high efficiency and low energy consumption. For catalytic processes such as Fischer-Tropsch synthesis, syngas must undergo deep removal of pollutants such as dust, tar, sulfides, chlorides, and alkali metals, while also requiring adjustment of the hydrogen-to-carbon ratio. Although traditional wet scrubbing purification is effective, it is accompanied by significant energy losses (sensible heat loss from syngas) and wastewater treatment issues.

[0004] Meanwhile, existing technologies typically combine units such as gasification, dust removal, tar removal, desulfurization and dechlorination, shift conversion, and decarbonization as relatively independent series modules. This approach lacks a synergistic optimization strategy based on the overall system, specifically in the following ways: it fails to deeply integrate the removal requirements of the purification units with gasification source suppression measures to fundamentally reduce impurity generation; it fails to adaptively reconstruct the purification bed sequence or operating parameters based on the dynamic changes in the syngas "impurity profile" caused by raw material fluctuations; and it fails to efficiently integrate the syngas component adjustment (ratio adjustment) process with the system's heat management.

[0005] Therefore, when dealing with complex biomass feedstocks with high chlorine, high alkali metal content, or large fluctuations in moisture content, existing technical routes cannot guarantee the long-term stability of syngas quality, which directly affects the lifespan and efficiency of downstream SAF synthesis catalysts and restricts the economic viability and large-scale development of BtL-SAF technology. Summary of the Invention

[0006] The purpose of this invention is to provide a method and system for preparing SAF syngas based on bubbling fluidized bed biomass gasification, thereby overcoming the shortcomings of existing technologies. Using biomass solid feedstock, biomass-derived fuel (RDF) containing biomass components, and organic waste liquid / organic hazardous waste as main raw materials, the invention employs bubbling fluidized bed (BFB) oxygen + gas + CO2 co-gasification, coupled with a synergistic control system of "feed-mixing-equivalent reaction input (ERI) estimation-zonal air distribution / multi-layer nozzles-hot catalytic filtration reforming-impurity fingerprinting reconfigurable deep purification-conversion / decarbonization linkage and CO2 reuse" to prepare high-purity syngas that meets the front-end requirements of Fischer-Tropsch (FT) or syngas-to-methanol / olefins-to-aviation kerosene (ATJ / OTJ, etc.), providing a reference for the industrialization of biomass-to-SAF production.

[0007] To achieve the above objectives, the technical solution of the present invention is as follows: On the one hand, the present invention provides a system for preparing SAF syngas from biomass gasification based on a bubbling fluidized bed, comprising a bubbling fluidized bed gasifier, a cyclone separator, a hot catalytic filtration-reforming integrated device, a reconfigurable dry deep purification unit, and a water-gas conversion and CO2 removal and reuse unit connected in sequence. The free plate area of ​​the bubbling fluidized bed gasifier is provided with at least two layers of gasifying agent nozzles on both sides along its axial direction. The reconfigurable dry deep purification unit is equipped with multiple switchable adsorption beds connected in parallel and / or in series, and is configured with an online analysis and program control system based on syngas impurity fingerprints. The water-gas conversion and CO2 removal and reuse unit is equipped with a CO2 return pipeline, which is used to transport part of the removed CO2 to the free plate area of ​​the bubbling fluidized bed gasifier.

[0008] The preparation system of this invention uses a bubbling fluidized bed as its core, and employs free plate separation to classify oxygen / gas pulses to suppress tar (source control); cyclone-followed hot catalytic filtration-reforming integration (process enhancement); online impurity fingerprinting identification and reconfigurable switching of the purification bed sequence (anti-fluctuation deep purification); and WGS / CO2 removal and reuse with steam addition linkage (component stabilization and thermal management coupling). While reducing wet scrubbing and wastewater, it obtains high-purity synthesis gas that can be directly fed into the front end of SAF synthesis such as FT or ATJ / OTJ.

[0009] In some other embodiments, the bubbling fluidized bed gasifier includes a gasifier body, which has a free plate zone, a reaction bed, an air distribution zone and a slag discharge section arranged sequentially from top to bottom inside. A synthesis gas outlet is provided on one side of the top of the free plate area, which is connected to the air inlet of the cyclone separator; a gasifying agent inlet is provided on the side wall of the air distribution area. The sidewall of the reaction bed is provided with a sealed pressurized feed port, and the bed is filled with bed material.

[0010] Biomass feedstock is dried and its particle size is controlled before being continuously fed into a bubbling fluidized bed gasifier in a sealed manner. Oxygen and steam are used as the main gasifying agents for bubbling fluidized bed gasification, and CO2 from the downstream CO2 removal unit is introduced as the third gasification medium in a set ratio. At least two layers of nozzles are set along the axial direction in the free plate zone of the gasifier, and graded pulse injection of oxygen pulse and steam pulse is performed to form an alternating atmosphere of mild partial oxidation and steam reforming reaction in the free plate zone, so as to inhibit tar formation and promote tar cracking.

[0011] In some other embodiments, the lower part of the cyclone separator is provided with a return leg, and the return leg is equipped with a return valve for returning the separated solid material to the reaction bed of the bubbling fluidized bed gasifier.

[0012] In some other embodiments, the hot catalytic filtration-reforming integrated device includes a gas collection chamber with a ceramic candle filter array inside. The array consists of multiple regularly arranged ceramic filter elements with catalytic reforming catalysts loaded on their surfaces, in order to achieve the integration of fine dust interception and tar / light hydrocarbon reforming.

[0013] One side of the gas collection chamber is equipped with an inlet manifold connected to the outlet of the cyclone separator, and the other side is equipped with an outlet manifold. A dust hopper is located at the bottom of the gas collection chamber, and a sealed dust discharge valve is installed on the dust hopper. A backflush header is located at the top of the gas collection chamber, and this header connects to multiple sets of pulse valves. The pulse valves and the ceramic candle filter array are interlocked with a differential pressure monitor and controller. Backflush is triggered when the pressure drop reaches a threshold. The backflush medium is steam, nitrogen, or a portion of the purified syngas, ensuring continuous operation and enabling online regeneration of the catalytic bed.

[0014] In some other embodiments, the reconfigurable dry deep purification unit includes a waste heat recovery device, a dry purification device, an online monitoring device, and a control device connected in sequence.

[0015] The dry purification device is a multi-bed sequence with program switching, including at least a COS hydrolysis catalytic bed, a desulfurization bed, a dechlorination bed, an alkali metal / trace metal collection bed, and a fine filtration device; The online monitoring device includes at least sensors for detecting H2S / COS, HCl, NH3, dust / aerosols, light hydrocarbons, and tar indicator signals. For different fingerprint modes, the device automatically switches the purification bed sequence and bypass priority (e.g., high-chlorine mode prioritizes increasing the dechlorination bed load and delaying the change; high-sulfur mode increases the pre-desulfurization bed and activates COS hydrolysis; high-alkali metal mode activates the alkali-capturing bed and increases the hot filter regeneration frequency), thereby achieving stable output with deep purification even under raw material fluctuations.

[0016] In some other embodiments, the system for preparing SAF syngas based on biomass gasification using a bubbling fluidized bed also includes a pharmaceutical plant organic waste liquid and organic hazardous waste disposal unit, which includes a waste liquid pretreatment and atomizing spray device, a secondary combustion chamber / oxidizer, a waste heat recovery device, a quenching device, and a flue gas purification device connected in sequence.

[0017] The flue gas purification device includes an alkali absorption unit, an activated carbon injection unit, and a bag filter or catalytic filtration unit.

[0018] It includes a multi-compartment metering and forced mixing and buffer homogenization structure, and calculates the equivalent reaction input (ERI) based on the characteristics of raw material moisture content, ash content and Cl / S, and uses ERI as a feedforward for oxygen, steam and recycled CO2 dosage, zoned air distribution setpoint and free plate zone pulse injection parameters.

[0019] The air chamber of the bubbling fluidized bed gasifier is divided into at least two zones and equipped with a variable porosity air distribution plate / spray cap and zone flow valve to achieve online adjustment of the bed gas velocity distribution and bed temperature distribution.

[0020] The fingerprint-reconfigurable deep purification unit includes a valve matrix and at least two sets of parallel-switchable purification beds. The valve matrix performs purification bed sequence reconfiguration and hot-state filtration backflushing frequency linkage control based on the online monitoring results of HCl, H2S / COS, NH3 and hot-state filtration pressure difference ΔP.

[0021] On the other hand, the present invention provides a method for preparing SAF syngas by biomass gasification based on bubbling fluidized bed, comprising the following steps: feeding pretreated biomass raw materials and gasifying agent into a bubbling fluidized bed gasifier for gasification reaction; In the free plate area of ​​the gasifier, the gasifying agent is injected in a staged pulse manner through the gasifying agent nozzles set on both sides, so that the area forms an alternating oxidation and reforming atmosphere, and a deep reforming reaction is carried out to obtain syngas. Syngas is separated by cyclone separator to obtain crude syngas and solid material; the solid material is returned to the gasifier, and the crude syngas enters the hot catalytic filtration-reforming integrated unit for filtration and catalytic reforming to obtain preliminarily purified syngas; The pre-purified syngas is fed into a reconfigurable dry deep purification unit, and the purification bed sequence is dynamically switched according to the impurity fingerprint monitored online for deep purification. The deeply purified syngas is subjected to water-gas shift reaction and CO2 removal treatment in sequence. By adjusting the amount of CO2 reused and the amount of steam added for the shift reaction in a coordinated manner, the H2 / CO molar ratio in the final syngas is stably adjusted to the target range required for SAF synthesis.

[0022] In some other embodiments, the reaction bed temperature of the bubbling fluidized bed gasifier is 750-900°C, and the temperature of the free plate zone is 800-1000°C. The vaporizing agent includes oxygen, water vapor, and recycled CO2; The gasification equivalence ratio (ER) is 0.15-0.35, and the mass ratio of gasification agent to biomass feedstock is 0.2-1.2. The pulse period of the graded pulse injection is 2–60 seconds, and the duty cycle is 1%–60%.

[0023] In some other embodiments, the water-gas shift reaction employs a single-stage or two-stage shift process; When performing Fischer-Tropsch (FT) synthesis, adjust the H2 / CO molar ratio of the synthesis gas to 1.8-2.3; The CO2 removal employs one or more combinations of chemical absorption, physical absorption, membrane separation, or pressure swing adsorption.

[0024] In some other embodiments, when treating organic waste liquid or hazardous waste from pharmaceutical plants, the operating temperature of the secondary combustion chamber / oxidation furnace is not lower than 850°C and the flue gas residence time is not less than 2 seconds; When handling hazardous waste with high halogen load, the operating temperature shall not be lower than 1100℃ and the residence time shall not be less than 2 seconds. The quenching device rapidly crosses the temperature range of 200-450°C for the flue gas, and in conjunction with the subsequent activated carbon injection and filtration unit, it inhibits the resynthesis of dioxins.

[0025] The beneficial effects of this invention are: (1) By actively regulating the oxygen / vapor pulse in the free plate, the source of tar is suppressed, which greatly reduces the load and operating cost of the deep purification at the back end; (2) The integrated design of hot catalytic filtration-reforming combines dust removal and tar catalytic recombination into a single unit, effectively reducing the cooling and reheating links in the traditional process and improving the overall thermal efficiency of the system; (3) The online identification based on impurity fingerprints and the reconfigurable switching of the purification bed sequence significantly enhance the system's adaptability to high-chlorine, high-alkali metals and raw materials with fluctuating composition, ensuring long-term stable operation; (4) By linking the control of WGS / CO2 removal and reuse with steam addition, the system thermal management is optimized and the carbon atom utilization efficiency is improved while achieving precise and stable control of the H2 / CO molar ratio; (5) Overall, the traditional wet washing unit is greatly reduced or even eliminated, and the demand for process water and wastewater treatment is reduced at the same time, making the system more suitable for large-scale continuous production and seamlessly connected with downstream SAF synthesis processes such as FT and ATJ. Attached Figure Description

[0026] The accompanying drawings, which form part of this invention, are used to provide a further understanding of the invention. The illustrative embodiments of the invention and their descriptions are used to explain the invention and do not constitute an improper limitation of the invention.

[0027] Figure 1 This is a diagram illustrating the overall technical roadmap of the system in Embodiment 1 of the present invention; Figure 2 This is a structural diagram of the bubbling fluidized bed gasifier in Embodiment 1 of the present invention; Figure 3 This is a structural diagram of the integrated hot-state catalytic filtration-reforming device in Embodiment 1 of the present invention; Figure 4 This is a flowchart of the high-temperature treatment and dioxin inhibition of hazardous waste / chlorine-containing pollutants in Example 1 of the present invention; Figure 5 This is a schematic diagram of the fingerprint-based purification and ratio linkage control logic in Embodiment 1 of the present invention; Figure 6 This is a comparison chart of tar / light hydrocarbon fluctuations between Application Example 1 and Comparative Example 1 of the present invention. Figure 7 This is a comparison chart of the H2 / CO stability of Application Example 1 and Comparative Example 2 of the present invention; Figure 8 This is a comparison diagram of the dechlorination bed breakthrough between Application Example 3 and Comparative Example 3 of the present invention; Figure 9 This is a diagram illustrating the effect of the "free plate staged pulse + hot catalytic filtration - reforming integration" on the stepwise reduction of tar concentration in Application Example 1 of this invention. Figure 10 This is a diagram illustrating the effect of "cyclone separation + hot catalytic filtration" on the stepwise reduction of dust / aerosol load in Application Example 1 of this invention; Figure 11 This diagram illustrates the effect of achieving closed-loop stable control of H2 / CO using the "WGS-CO2 removal and reuse-steam addition linkage" method in Application Example 1 of this invention. Detailed Implementation

[0028] The following examples are for illustrative purposes only and should not be construed as limiting the scope of the invention. Specific conditions are not specified in the examples; they were performed under conventional conditions or conditions recommended by the manufacturer. Unless otherwise specified, all components used are commercially available conventional products.

[0029] Existing gasification syngas purification technologies generally employ fixed "gasification-dust removal-desulfurization-conversion" series modules, focusing on back-end processing and independent unit operation. They lack overall optimization for tar source suppression, dynamic adaptation of the purification process, and cross-unit collaborative control. This makes it difficult to consistently produce clean syngas that meets the requirements of high-end synthesis (such as SAF) when processing complex raw materials. Known patents mostly focus on local structural or single-function improvements, failing to form a closed-loop control framework with gasification state as feedforward and impurity signals as feedback, and also failing to achieve deep coupling of source tar suppression, online reconstruction of the purification sequence, and component / heat linkage regulation. This invention aims to overcome the limitations of existing segmented processing through integrated component and strategy design, achieving a significant improvement in overall system performance. Specifically, this invention explicitly improves the structure and control strategies of the following key components / units, and achieves a synergistic effect through cross-unit closed-loop linkage.

[0030] The improvement target of this invention is not the abstract "syngas system," but rather the following specific components and their control interfaces: ① Feed-mixing-sealing feed assembly; ② Zoned air distribution / variable pore air distribution plate assembly; ③ Free plate zone multi-layer oxygen / gas / CO2 pulse nozzle assembly; ④ Cyclone return leg and return valve assembly; ⑤ Hot catalytic filtration-reforming integrated assembly; ⑥ Reconfigurable dry deep purification valve group matrix; ⑦ WGS / CO2 removal and reuse linkage ratio assembly; ⑧ Organic waste liquid / organic hazardous waste secondary combustion chamber and quench purification assembly. The technical effects of the above components are not a simple summation of their individual functions, but rather form a closed loop around the same technical goal of "reducing syngas impurity load fluctuations, stabilizing H2 / CO, and protecting downstream SAF synthesis catalysts."

[0031] Specifically, the feed-mixing assembly first stabilizes the dry-based carbon input and Cl / S / Ash load through ERI feedforward, reducing disturbances in bed temperature and equivalence ratio; the zoned air distribution assembly then distributes this relatively stable disturbance to different bed regions to prevent channeling, flow deviation, and localized over-oxygenation; the pulse nozzles in the free plate area perform peak clipping based on tar / light hydrocarbon signals, making the load at the downstream hot catalytic filter inlet predictable; the pressure difference and backflushing status of the hot catalytic filter assembly are then fed back to the upstream nozzles and the purification bed sequence, so that tar generation, filter element carbon buildup, and adsorption bed penetration are no longer handled independently by individual units, but are reduced by system-wide linkage.

[0032] Therefore, the synergistic results of this invention are as follows: under the same raw material and gas production conditions, the peak value of tar, light hydrocarbon fluctuation, dust penetration, peak value of HCl and H2 / CO deviation are reduced simultaneously. If the multi-layer nozzle, ceramic filter, desulfurization / dechlorination bed and WGS are simply connected in series in a conventional manner, the above indicators can only be improved locally within their respective units, and the effects of fluctuation reduction, load transfer and downstream catalyst protection across units cannot be obtained.

[0033] (1) Feeding-mixing-sealing feeding assembly: Add a "multi-compartment metering + forced mixing + buffer homogenization compartment + double lock hopper (or spiral seal) continuous feeding" structure to the raw material pretreatment section; estimate the equivalent reaction input (ERI) by online moisture content / ash content / chlorine and sulfur indicators, and use ERI as the feedforward amount for gasification agent ratio, zoned air distribution and free plate area pulse injection, which significantly reduces the transient temperature / equivalent ratio and tar peak caused by raw material fluctuations.

[0034] (2) Zoned air distribution and variable porosity air distribution plate assembly: The air chamber is divided into at least two zones (preferably three sections: main gasification zone / oxygen supplementation zone / stable flow zone). The air distribution plate adopts an adjustable porosity or replaceable spray cap structure, and is used in conjunction with zoned flow valves to achieve controllable "bed reaction intensity - fluidization uniformity - carrying capacity", providing a stable bed base state for subsequent pulse control of tar in the free plate zone.

[0035] (3) Multi-layer pulse injection assembly in free plate area: 2-4 layers of nozzle array (oxygen / gas / CO2 three media can be switched) are arranged along the axis in the free plate area. The alternating atmosphere of "short-term mild partial oxidation + steam reforming" is executed by high-speed pulse valve. The pulse cycle / duty cycle / injection volume is adjusted in conjunction with the downstream tar indicator, C2-C6 light hydrocarbon ratio and catalytic filter pressure difference ΔP to achieve source tar reduction and filter load reduction.

[0036] (4) Hot-state catalytic filtration-reforming integrated component: After cyclone treatment, the filter element is kept at 450–850°C before entering the ceramic candle (or honeycomb) catalytic filter. The filter element surface / pores are loaded with Ni-based or Ni-based materials. Fe steam reforming components; setting "ΔP threshold triggered backflushing + parallel standby filter chamber / bypass switching" to ensure continuous gas supply, and prioritizing the extraction of backflushing steam from waste heat recovery steam generation to achieve energy-purification synergy.

[0037] (5) Impurity fingerprinting reconfigurable dry deep purification component: Online monitoring points for H2S / COS, HCl, NH3, aerosol / dew point / pressure drop are arranged before and after the fixed bed such as desulfurization / dechlorination / alkali capture / fine filtration. The bed sequence and bypass can be reconfigurably switched through the valve group matrix. When the high chlorine / high sulfur / high alkali metal mode is identified, the bed sequence and hot filtration regeneration frequency are automatically adjusted to minimize the fluctuation of outlet impurities within the catalyst tolerance range.

[0038] (6) WGS / Decarbonization-CO2 Recycling-Steam Addition Linkage Control Component: The steam addition amount in the conversion section is linked with the CO2 recycling amount to keep H2 / CO stable within the target range; at the same time, the recovered CO2 is used as the third gasification medium to participate in temperature stabilization and slag suppression, forming a synergistic closed loop of "ratio adjustment-thermal management-carbon efficiency".

[0039] (7) Organic waste liquid / organic hazardous waste co-treatment and dioxin inhibition component: chlorine-containing organic waste liquid, pharmaceutical hazardous waste, etc. meet the 3T conditions (≥850℃, residence ≥2s, oxygen content ≥6%) in an independent high-temperature oxidation / incineration unit, and adopt high-temperature dust removal at ≥550℃ + energy recovery followed by rapid cooling of alkaline solution to <200℃ and ≤1s to cut off the low-temperature resynthesis window of dioxins; the recovered heat is used for gasification drying / steam generation / backflushing to avoid cross-contamination caused by series connection with syngas purification.

[0040] The solution of the present invention will be further described below with reference to specific embodiments: Example 1 This embodiment provides a system for producing SAF syngas from biomass gasification based on a bubbling fluidized bed gasifier. The system includes a pretreatment unit, a bubbling fluidized bed (BFB) gasifier, a cyclone separator, a hot catalytic filtration-reforming integrated unit, a reconfigurable dry deep purification unit, a WGS / CO2 removal and reuse unit, and a compression and stabilization unit connected in sequence. The pretreatment unit is used to dry and crush the biomass feedstock. The BFB gasifier receives the pretreated feedstock and performs the gasification reaction; the free plate area of ​​the BFB gasifier is equipped with a staged oxygen / gas pulse injection device. The inlet of the cyclone separator is connected to the outlet of the BFB gasifier to remove large particles from the crude syngas. The inlet of the hot catalytic filtration-reforming integrated unit is connected to the outlet of the cyclone separator for high-temperature filtration, dust removal, and catalytic reforming of residual tar and light hydrocarbons in the syngas. The inlet of the reconfigurable dry deep purification unit is connected to the hot catalytic filtration-reforming integrated unit. The outlet of the unit is equipped with multiple switchable adsorption bed programs based on online impurity fingerprint analysis for deep removal of sulfur, chlorine, and alkali metal impurities. The inlet of the WGS / CO2 removal and reuse unit is connected to the outlet of the reconfigurable dry deep purification unit for adjusting the H2 / CO molar ratio of the syngas and removing CO2. A pipeline is also provided to return some of the removed CO2 to the free plate area of ​​the BFB gasifier. The inlet of the compression and stabilization unit is connected to the outlet of the WGS and CO2 removal coupling unit for pressurizing and stably delivering the purified and conditioned syngas to the downstream Fischer-Tropsch (FT) or ATJ synthesis section.

[0041] like Figure 2As shown, the bubbling fluidized bed gasifier includes the gasifier body and its internal components arranged from top to bottom as follows: a free plate zone (suspension section), a bed (bubbling fluidized section), an air distribution zone, and a slag discharge zone. On the two side walls of the free plate zone, nozzle layers 1, 2, and 3 are respectively arranged from top to bottom. All three nozzle layers are used for oxygen / gas, resulting in a reaction temperature of 800-1000℃ in the free plate zone. Through pyrolysis and steam reforming, the tar content is reduced, and the yield of effective components (H2 and CO) in the syngas is increased. A syngas discharge port is also provided at the top of one side of the free plate zone, connected to the feed port of a cyclone separator. After separation in the cyclone separator, the syngas produces crude syngas and syngas slag. The crude syngas enters a hot catalytic filtration-reforming integrated unit for processing, while the syngas slag is returned to the bed through a return valve on the return leg.

[0042] The bed has a sealed pressurized feed port on its side wall. This port, along with existing double-lock hopper and screw / pneumatic conveying devices, transports raw materials with a particle size of 0.5-29 mm into the bed of the bubbling fluidized bed gasifier. The bed contains bed material, which can be selected from existing materials such as olivine, dolomite, spinel, and Ni / Fe / alkaline earth. The reaction temperature within the bed is 750-900℃. The side wall of the air distribution zone has a gasifying agent inlet, and the top of the air distribution zone has an air distribution plate or air cap. The gasifying agent (O2 + steam or circulating CO2) entering through the gasifying agent inlet is evenly distributed into the bed, thus facilitating the full reaction of the raw materials. The slag discharge section uses water-sealed cooling, and a slag discharge valve is located at the bottom of the slag discharge section.

[0043] like Figure 3 As shown, the integrated hot-state catalytic filtration-reforming unit includes a synthesizer gas collection chamber and a ceramic candle filter array installed inside it. The ceramic candle filter array includes several regularly arranged ceramic filter elements and catalysts (existing Ni or Ni-Fe reforming catalyst components can be selected) supported on their surfaces. An inlet manifold is provided on one side of the synthesizer gas collection chamber, which is connected to the crude synthesis gas pipeline after cyclone separation (equipped with a bypass switching valve group) to transport the crude synthesis gas after cyclone separation to the ceramic candle filter array for purification treatment.

[0044] An outlet manifold is located on the other side of the synthesizer's gas collection chamber. The purified synthesis gas is discharged from the outlet manifold into the clean hot gas outlet for waste heat recovery / purification / WGS treatment. An ash hopper is located at the bottom of the synthesizer's gas collection chamber, and a sealed ash discharge valve is installed on the ash hopper.

[0045] A backflush header is located at the top of the synthesizer's gas collection chamber. This header connects to multiple sets of parallel pulse valves. Both the pulse valves and the ceramic candle filter array are connected to a differential pressure monitor and a controller / interlock. When the differential pressure exceeds a set critical real-time differential pressure value, the ceramic candle filter array automatically switches to backflush mode. The controller / interlock opens the corresponding pulse valve in the backflush header to backflush the ceramic candle filter array until the real-time differential pressure is less than the set critical real-time differential pressure value. The backflush mode then ends, and the system switches to filtration mode. The backflush medium is steam, nitrogen, or a portion of the purified synthesis gas, ensuring continuous operation and enabling online regeneration of the catalytic bed.

[0046] The reconfigurable dry deep purification unit comprises a waste heat recovery device, a dry purification device, and an online monitoring and control device connected in sequence. The waste heat recovery device is used to generate steam from syngas via heat exchange for gasification and conversion. The dry purification device is a switchable multi-bed sequence, including at least a COS hydrolysis catalytic bed (if necessary), a desulfurization bed (containing desulfurization catalysts such as ZnO / iron-based / composite metal oxides), a dechlorination bed (containing dechlorination adsorbents such as alkaline alumina / calcium-based adsorbents / carbonate-supported adsorbents), an alkali-capturing metal / trace metal bed (containing aluminosilicate / molecular sieve trapping agents), and a fine filtration device (for deep interception of aerosols and ultrafine dust). The online monitoring device includes: H2S / COS, HCl, NH3, dust / aerosol (or dew point / conductivity / pressure drop indicators), light hydrocarbon (C2–C6), and tar indicator signal devices.

[0047] The online monitoring device classifies the impurity profiles of the raw materials and syngas into at least three categories of "impurity fingerprint patterns" based on the monitoring results, such as... Figure 5 As shown, the modes include high-chlorine mode (Mode 1), high-sulfur mode (Mode 2), high-alkali metal mode (Mode 3), and normal / high-tar mode (Mode 0). For different fingerprint modes, the control device automatically switches the purification bed sequence and bypass priority in the dry purification unit. Specifically, in high-chlorine mode, the dechlorination bed load is increased first, and the change is delayed; in high-sulfur mode, the desulfurization bed is pre-positioned and COS hydrolysis is activated; in high-alkali metal mode, the alkali-capturing bed is activated and the hot filtration regeneration frequency is increased, thereby achieving stable output of deep purification under raw material fluctuations.

[0048] The WGS / CO2 removal and reuse unit comprises a water-gas shift (WGS) unit and a CO2 removal unit connected in sequence. The WGS unit performs water-gas shift on the purified syngas (using a single-stage or two-stage high / low temperature combination), adjusting the H2 / CO ratio to the target range: for FT: H2 / CO = 1.8-2.3; for ATJ / OTJ front-end: 0.8–1.2 or other ranges can be set according to the target route. The CO2 removal unit employs one or a combination of chemical absorption, physical absorption, membrane separation, or PSA. The removed CO2 is returned to the bubbling fluidized bed gasifier as the third gasification medium according to a set ratio, and is linked to the steam injection rate in the shift section for control, achieving coupling of "ratio adjustment—thermal management—carbon efficiency".

[0049] The workflow of the above-mentioned system for producing SAF syngas from biomass gasification based on a bubbling fluidized bed is as follows: Figure 1 As shown, the details are as follows: (1) Biomass feedstock or biomass solid waste derived fuel (RDF) undergoes pretreatment in the pretreatment unit, including drying, crushing and screening, to achieve suitable particle size and moisture content. The pretreated feedstock is then sealed and fed into the bubble fluidized bed (BFB) gasifier through a feeding device equipped with a double gate hopper and spiral seal.

[0050] (2) The pretreated raw material reacts with oxygen, steam and partially recycled CO2 mixed gasifying agent introduced from the bottom in a bubble fluidized bed (BFB) gasifier to generate crude syngas. In the free plate zone of the gasifier, online signal closed-loop control is carried out through multi-layer segmented (2-4 layers) inclined injection ports, with alternating oxygen pulses and steam pulses, to actively suppress tar formation from the reaction source.

[0051] (3) After leaving the gasifier, the high-temperature crude syngas carrying particulate matter first enters the cyclone separator to remove most of the large-sized particles. Then, the gas enters the hot catalytic filtration-reforming integrated unit, where deep dust removal and catalytic reforming of residual tar and light hydrocarbons are completed simultaneously. This unit can be regenerated by backflushing to achieve process enhancement.

[0052] (4) The high-temperature purified gas from the hot catalytic filtration-reforming integrated unit enters the waste heat recovery unit to generate steam. The generated steam is used to supply gasification, water-gas conversion and backflushing processes. The cooled gas enters the fingerprint-based reconfigurable dry deep purification unit. The system identifies specific impurity "fingerprints" (such as sulfur, chlorine, and alkali metal species) in the gas online and dynamically switches the purification bed sequence composed of various adsorbents (such as desulfurization, dechlorination, alkali capture, and fine filtration) to cope with raw material fluctuations and achieve stable and deep removal of impurities.

[0053] (5) The purified syngas enters the water-gas shift (WGS) and CO2 removal coupling unit (which can be a single stage or a two-stage system of high-temperature HTS and low-temperature LTS connected in series). The H2 / CO molar ratio is precisely adjusted to the target value (e.g., 2.0 ± 0.1) through the reaction. Most of the CO2 in the shifted gas is removed by CO2 removal (e.g., absorption, microbubble separation, or pressure swing adsorption PSA). A portion of the CO2 is separated and returned to the gasifier, which is linked with the steam injection to stabilize the bed temperature and improve carbon utilization efficiency.

[0054] (6) The high-purity, controllable-proportion syngas that meets the requirements is compressed and stabilized, and then stably transported to the front end of the downstream synthesis section of sustainable aviation fuel (SAF) such as Fischer-Tropsch synthesis (FT) or ATJ or OTJ.

[0055] To further improve waste heat recovery and steam resource utilization, the biomass gasification system for producing SAF syngas based on a bubbling fluidized bed provided in this embodiment can also integrate a co-treatment module for pharmaceutical plant organic waste liquid and organic hazardous waste (containing halogenated / chlorinated organics). Through high-temperature and complete combustion in a secondary combustion chamber / oxidizer (≥850℃, ≥2s; high halogen load can be increased to ≥1100℃, ≥2s), waste heat recovery and rapid cooling quickly cross the 200–450℃ dioxin regeneration window, and adopt a combination of alkali absorption + activated carbon injection + bag / catalytic filtration for purification, the system achieves the inhibition of chlorinated pollutants and dioxins and energy recovery.

[0056] High-temperature treatment and dioxin suppression process for hazardous waste / chlorine-containing pollutants, as follows: Figure 4 As shown, pharmaceutical plant organic waste liquid and organic hazardous waste (which may contain halogenated / chlorinated organic matter) undergo homogenization, desalination, and dehydration pretreatment. Then, through an injection / metering device and oxygen / oxygen-enriched air, it is introduced into a secondary combustion chamber / oxidizer for high-temperature, complete combustion (≥850℃, ≥2s; high halogen load can be increased to ≥1100℃, ≥2s). The resulting waste heat and steam are recovered. Simultaneously, the steam enters a quenching device to rapidly cross the 200–450℃ dioxin regeneration window, and is purified using a combination of alkali absorption, activated carbon injection, and bag / catalytic filtration. Furthermore, the generated steam is collected through a steam header and enters a system based on a bubbling fluidized bed for biomass gasification to produce SAF syngas for gasification, purification, or proportioning. Ultimately, this achieves the inhibition of chlorinated pollutants and dioxins, as well as energy recovery.

[0057] Example 2 This embodiment provides a method for preparing SAF syngas based on biomass gasification using a bubbling fluidized bed, including the following steps: Step 1: Raw material pretreatment and sealed feeding Equivalent Reaction Input (ERI) Estimation and Feedforward Control: Before feeding, the characteristics of the feedstock, such as moisture content, ash content, and Cl / S, are acquired online / offline. The ERI (characterizing equivalent gasifiable carbon input, volatile matter intensity, and oxygen / steam demand) is calculated and used as a feedforward for oxygen, steam, and (optional) CO2 dosage and zoned air distribution settings to reduce the impact of feedstock fluctuations on bed temperature, ER, and peak tar content.

[0058] The raw materials are sawdust, straw, agricultural and forestry residues, garden waste, biomass-derived fuel (RDF), organic hazardous waste (including high-COD liquids), or a mixture thereof; waste heat / low-pressure steam drying is used to achieve a moisture content of 5–20 wt%; crushing and screening yield a particle size of 0.5–20 mm; a double-lock hopper (or spiral seal) continuous feeding system is used to feed the gasifier (at atmospheric pressure or pressurized 0.1–3.0 MPa); for example, a multi-compartment metering and forced mixer is set before the lock hopper, and a buffer homogenization compartment is set to suppress instantaneous feeding fluctuations; the lock hopper pressure is linked to the return CO2 / nitrogen sealing gas to ensure continuous and stable feeding under pressurized conditions.

[0059] Step 2: Bubbling fluidized bed oxygen-gas (optional CO2) combined gasification The gasifying agents are oxygen and water vapor; recycled CO2 can be introduced as a third gasification medium; the bed temperature is 750–900℃, and the free plate zone temperature is 800–1000℃; the equivalence ratio (ER) is 0.15–0.35; the steam / biomass mass ratio is 0.2–1.2; the bed material uses inert or weakly catalytic materials such as olivine / dolomite / magnesium aluminum spinel, and Ni, Fe, or alkaline earth metal modified bed materials can be added online and recycled. The gasifier can operate at atmospheric pressure or pressurized pressure of 0.1–3.0 MPa; for example, by setting up zoned air chambers and variable porosity air distributors / spray caps, oxygen, steam, and recycled CO2 are introduced into the bed in zones, forming a controllable gas velocity distribution and bed temperature distribution, reducing channeling and local over-oxidation.

[0060] Step 3: Free plate classification of oxygen / vapor pulse tar suppression At least two layers of nozzles (preferably 2–4 layers) are arranged axially in the free plate zone. Each layer of nozzles can perform oxygen pulses or steam pulses. Oxygen pulses: briefly increase the local mild oxidation intensity and temperature, causing heavy tar to crack into smaller molecules that are easier to reform. Steam pulses: enhance the driving force of steam reforming and inhibit local slagging, stabilizing the reaction atmosphere in the free plate zone. The pulse period, duty cycle and injection volume are dynamically adjusted according to the "tar fingerprint and light hydrocarbon ratio" obtained by online monitoring (see online monitoring in step E), so that the free plate zone forms an alternating "mild partial oxidation - steam reforming" reaction atmosphere, reducing tar generation from the source.

[0061] Step 4: Cyclone-fed hot catalytic filtration-reforming integrated system After large particles are removed by cyclone separation, the crude syngas is maintained at 450–850℃ and enters the hot catalytic filtration unit. The hot catalytic filtration unit is a ceramic candle or honeycomb filter. The surface or pores of the filter material are loaded with Ni-based or Ni-Fe steam reforming catalytic components, so that fine dust interception and tar / light hydrocarbon catalytic reforming can be completed in the same unit. Backflushing regeneration and bypass switching are set: when the pressure drop reaches the threshold, backflushing is triggered. The backflushing medium is steam, nitrogen or part of the purified syngas, ensuring continuous operation and realizing online regeneration of the catalytic bed.

[0062] Step 5: Online Impurity Fingerprint Identification and Reconfigurable Deep Purification of the Purification Bed Sequence Waste heat recovery: Syngas is heated to generate steam for gasification and conversion; the dry purification unit employs a switchable multi-bed sequence, including at least: a COS hydrolysis catalytic bed (if necessary), a desulfurization bed (ZnO / iron-based / composite metal oxide), a dechlorination bed (alkaline alumina / calcium-based adsorbent / carbonate-supported adsorbent), an alkali-capturing metal / trace metal bed (aluminosilicate / molecular sieves, etc.), and a fine filtration unit (deep interception of aerosols and ultrafine dust); online monitoring includes at least: H2S / COS, HCl, NH3, dust / aerosol (or dew point / conductivity / pressure drop indication). In addition to light hydrocarbons (C2–C6) and tar indicator signals; based on the monitoring results, the impurity spectrum of the feedstock and syngas is divided into at least three types of "impurity fingerprint patterns": high chlorine mode, high sulfur mode, and high alkali metal mode (which can be expanded to high nitrogen / high tar mode); for different fingerprint patterns, the purification bed sequence and bypass priority are automatically switched (for example: in the high chlorine mode, the dechlorination bed load is increased first and the change is delayed; in the high sulfur mode, the desulfurization bed is pre-positioned and COS hydrolysis is activated; in the high alkali metal mode, the alkali scavenging bed is activated and the hot filtration regeneration frequency is increased), thereby achieving stable output of deep purification under feedstock fluctuations.

[0063] Step 6: WGS / CO2 removal and reuse linkage ratio adjustment The purified syngas undergoes water-gas shift conversion (single-stage or two-stage high / low temperature combination) to adjust the H2 / CO ratio to the target range: for FT: H2 / CO = 1.8–2.3; for ATJ / OTJ front end: 0.8–1.2 or other ranges can be set according to the target route; CO2 removal adopts one or a combination of chemical absorption, physical absorption, membrane separation or PSA; the removed CO2 is returned to step 2 as the third gasification medium according to the set ratio, and is linked with the steam injection rate of the shift section to achieve "adjustment ratio - thermal management - carbon efficiency" coupling; after obtaining high-cleanliness syngas that meets the requirements of SAF synthesis front end, it is compressed and sent to downstream synthesis.

[0064] Application Example 1 This application example provides a method for producing high-cleanliness syngas (target H2 / CO≈2.0) for Fischer-Tropsch synthesis of sustainable aviation fuel (SAF). The specific steps are as follows: Raw materials: sawdust / straw = 7 / 3 (mass ratio), moisture content 10 wt%, particle size 1–10 mm.

[0065] Gasification and pulsed strategy: BFB bed temperature 860℃, free plate zone temperature 920℃; ER=0.25; steam / biomass=0.6.

[0066] The free plate area has three layers of nozzles: the first layer is oxygen pulse, the second layer is steam pulse, and the third layer is switchable; the pulse period is 2–20 s, the duty cycle is 5–40%, and the tar indicator signal and the C2–C6 ratio are used as control inputs.

[0067] Hot catalytic filtration: After cyclone, the gas enters the catalytic candle filter at 650–720℃, with the element loaded with Ni-based reforming catalytic components; when the pressure drop reaches the threshold, backflushing (steam or purified gas) is triggered and bypass switching is maintained to keep the gas supply continuous.

[0068] Fingerprint-based purification: Online monitoring of H2S / COS and HCl. The normal bed-entry sequence is: COS hydrolysis → ZnO desulfurization → dechlorination → alkali capture → fine filtration.

[0069] Adjustment ratio and reuse: The two-stage WGS adjusts the H2 / CO ratio to 2.0±0.1; CO2 is removed to 2–5 vol%, of which 30–70% is returned to the gasifier and the external steam fluctuation is adjusted accordingly.

[0070] Results: It can stably output high-cleanliness synthesis gas that is compatible with the front end of FT synthesis, and the system energy is used to generate steam from waste heat to achieve internal circulation, reducing the need for wet scrubbing.

[0071] Comparative Example 1 Comparative Example 1 (Routine Operation): Unlike Application Example 1, this example uses fixed wet-based feeding, single-zone air distribution, continuous low-flow secondary air / steam injection in the free plate zone, and a fixed clean bed sequence. It does not employ ERI feedforward, multi-compartment buffer homogenization, zoned air distribution, or oxygen / steam pulse closed-loop control based on tar / light hydrocarbon signals.

[0072] Depend on Figure 6 It can be seen that under operating conditions 1-3, the comprehensive fluctuation index of tar / light hydrocarbon in Application Example 1 is significantly lower than that in Comparative Example 1. This indicates that the synergistic control of "feed buffer homogenization - zoned air distribution - free plate zone pulse reforming" is not the effect of a single component, but rather reduces feed disturbance, stabilizes the bed fluidization ground state, and dynamically reduces the peak value of tar in the free plate zone, making the inlet load of subsequent hot catalytic filtration more stable.

[0073] Comparative Example 2 Comparative Example 2 (Conventional WGS): Unlike Application Example 1, the shift section uses a fixed steam injection rate, a fixed shift bypass ratio, and a fixed CO2 removal load, without linkage adjustment based on online H2 / CO, CO2 removal rate, and recycled CO2 flow rate.

[0074] Depend on Figure 7 It can be seen that when there is a disturbance in the feed composition and moisture content, the H2 / CO molar ratio of Comparative Example 2 deviates from the target value and fluctuates periodically; Application Example 1 uses the linkage control of WGS steam injection, CO2 removal and CO2 reuse to stabilize the H2 / CO ratio at around 2.0±0.1, indicating that a synergistic closed loop of "component adjustment-temperature adjustment-carbon efficiency" is formed between the ratio control unit and the gasification heat management unit.

[0075] Comparative Example 3 Comparative Example 3 (Fixed Bed Sequence): Unlike Application Example 3, the dry purification device uses a fixed COS hydrolysis-desulfurization-dechlorination-alkali capture-fine filtration series bed. It does not reconstruct the bed sequence based on online HCl, H2S / COS, NH3, dust / aerosol and hot filtration pressure difference, nor does it change the hot filtration backflushing frequency and upstream pulse jet strategy.

[0076] Depend on Figure 8 It can be seen that under the high chlorine / high alkali metal fluctuation conditions, the dechlorination bed in Comparative Example 3 showed a breakthrough trend earlier; Application Example 3, through high chlorine mode identification, parallel / pre-positioning of dechlorination beds, early commissioning of alkali-collecting beds, and linkage of hot filtration backflushing frequency, can delay HCl breakthrough and reduce the risk of downstream catalyst poisoning, demonstrating the synergistic effect of "impurity fingerprint identification - bed sequence reconstruction - upstream source adjustment".

[0077] Application Example 2 This application example provides a method for producing adjustable ratio syngas (target H2 / CO≈1.0) for alcohol-based jet fuel (ATJ) / oil-based jet fuel (OTJ). The specific steps are as follows: Raw materials: Garden waste and wood chips are mixed in a mass ratio of 6:4, with a moisture content of 15 wt% and a particle size of 0.5-15 mm.

[0078] Gasification: bed temperature 820℃, free plate zone temperature 880–950℃; equivalence ratio ER=0.20; steam / biomass=0.45.

[0079] Pulse strategy: Using "light hydrocarbons (C2–C6) + NH3" as the main control input: when NH3 is too high, increase the oxygen pulse intensity to promote cracking; when light hydrocarbons are too high, increase the vapor pulse ratio to promote reforming.

[0080] Purification and balancing: A single-stage water-gas shift reaction (WGS) or bypass shift reaction is used to control the H2 / CO ratio at 0.9–1.1; the CO2 removal rate is set by the downstream route, and CO2 is reused for temperature stabilization and slagging reduction.

[0081] Results: Achieved online adjustability of H2 / CO over a wide range, adapting to the switching requirements of different synthetic routes.

[0082] Application Example 3 This application example provides a method for robust operation of feedstocks with high chlorine / high alkali metal fluctuations (RDF containing biomass components), with the specific steps as follows: Raw materials: biomass waste-derived fuel RDF + straw (mass ratio 6:4), with significant fluctuations in chlorine content and high ash content.

[0083] Fingerprint classification and reconfigurable switching: When HCl enters the high-level range, switch to "high-chlorine mode": the dechlorination bed is placed in front and parallel beds are put into operation; at the same time, the oxygen pulse intensity is reduced and the steam pulse ratio is increased to suppress the risk of chloride aerosols and slagging.

[0084] When abnormal aerosol / pressure drop is detected, switch to "high alkali metal mode": prioritize alkali capture bed, increase the frequency of hot filter regeneration and shorten the backflushing cycle.

[0085] When sulfide levels rise, switch to "high sulfur mode": activate COS hydrolysis pre-processing and increase the desulfurization bed load.

[0086] Results: Even under complex raw material conditions, the purity and composition of the syngas can still be maintained, meeting the requirements for continuous operation of downstream synthesis units.

[0087] Application Example 4 This application example provides a method for the disposal of organic waste liquid / organic hazardous waste and the inhibition of dioxins in a pharmaceutical plant. The specific steps are as follows: To ensure complete suppression of dioxins (PCDD / F) throughout the treatment process, the preferred treatment module employs a combined process of "high-temperature full oxidation—waste heat recovery—rapid cooling—alkali absorption—activated carbon injection—bag filter / catalytic filtration": (a) High-temperature full oxidation: Organic waste liquid / hazardous waste is desalinated (optional), homogenized and dehydrated as necessary, and then atomized and sprayed into the secondary combustion chamber / oxidizer; it is fully oxidized under sufficient oxygen and optimized turbulent mixing conditions. Under normal operating conditions, the temperature is guaranteed to be ≥850℃ and the residence time is ≥2 s; when the halogen / chlorine load is high, the temperature is increased to ≥1100℃ and the residence time is ≥2 s, while maintaining sufficient excess oxygen and mixing intensity.

[0088] (b) Rapid cooling: After waste heat recovery, a rapid cooling device is installed to allow the flue gas to quickly cross the 200–450°C range in order to reduce the regeneration of dioxins; rapid cooling can be achieved by spray rapid cooling tower or heat exchange rapid cooling device, and priority should be given to controlling the residence time in this range to the minimum value that can be achieved by the project.

[0089] (c) Inhibition of chlorine-containing pollutants and catalytic sites: Alkali absorption (such as NaOH / Ca(OH)2, etc.) is set to preferentially remove HCl and reduce the activity of metal chlorination; then activated carbon is sprayed to adsorb PCDD / F and its precursors; bag filter or catalytic filter captures fly ash and weakens the catalytic effect of transition metal sites such as Cu / Fe on the generation / regeneration of dioxins.

[0090] (d) Energy recovery and system coupling: The waste heat of the treatment module is preferably recovered into steam through a waste heat boiler and supplied to gasification steam, change steam or hot filter backflushing medium, thereby reducing the external energy consumption of the system.

[0091] When the system needs to co-process organic waste liquid / organic hazardous waste (which may contain chlorinated organics) from pharmaceutical plants, a secondary combustion chamber / oxidizer can be set up to achieve high-temperature and complete combustion. It can also be equipped with waste heat recovery, rapid cooling to quickly cross the 200–450℃ temperature window, and combined purification of alkali absorption + activated carbon injection + bag filter (or catalytic filter) to inhibit the regeneration of dioxins and reduce the emission of chlorinated pollutants. The recovered steam can be used for gasification and conversion to further reduce the system's external energy consumption.

[0092] Figure 9 – Figure 11 To illustrate the operational results, key effects and comparisons from implementation cases are provided. This serves to demonstrate the technical effectiveness; in actual projects, measured data can be substituted according to project boundaries and testing standards.

[0093] like Figure 9 It is known that the "oxygen / vapor staged pulse" in the free plate zone reduces the generation of heavy tar and promotes cracking at the source; after the cyclone enters the hot catalytic filtration-reforming integrated unit, the residual tar and C2-C6 light hydrocarbons are further converted into CO and H2, thereby significantly reducing the risk of downstream cold-end condensation and coking.

[0094] like Figure 10 It can be seen that after the cyclone removes large particles, the hot filtration deeply intercepts fine particles and aerosols, and maintains a long-term stable pressure drop through backflushing regeneration, which meets the dust load requirements of the subsequent dry bed and compressor.

[0095] Based on impurity fingerprints such as HCl, H2S / COS, alkali metals, and dust load, a reconfigurable switching bed sequence can be achieved to realize stable and deep removal of HCl and sulfides, while suppressing the entry of alkali metal salt aerosols into the downstream catalyst and heat exchange system. Figure 11It can be seen that by using the WGS-CO2 removal and reuse-hydrogen replenishment (or bypass conversion) linkage closed-loop control, the H2 / CO molecular molar ratio can be stabilized within the set value and control band.

[0096] Organic waste liquid / organic hazardous waste and dioxin suppression: The treatment module employs a combination of high-temperature full oxidation + rapid cooling across the window + alkali absorption / activated carbon / bag filter (or catalytic filter) to reduce HCl and PCDD / F and capture fly ash containing transition metals, thereby suppressing dioxin formation / regeneration; waste heat recovery provides steam and heat to the system (see...). Figure 4 ).

[0097] The above are merely preferred embodiments of the present invention and are not intended to limit the present invention. Various modifications and variations can be made to the present invention by those skilled in the art. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the scope of protection of the present invention.

Claims

1. A system for producing SAF syngas based on biomass gasification using a bubbling fluidized bed, characterized in that, It includes a bubbling fluidized bed gasifier, a cyclone separator, a hot catalytic filtration-reforming integrated device, a reconfigurable dry deep purification unit, and a water-gas conversion and CO2 removal and reuse unit connected in sequence. The free plate area of ​​the bubbling fluidized bed gasifier is provided with at least two layers of gasifying agent nozzles on both sides along its axial direction. The reconfigurable dry deep purification unit is equipped with multiple switchable adsorption beds connected in parallel and / or in series, and is configured with an online analysis and program control system based on syngas impurity fingerprints. The water-gas conversion and CO2 removal and reuse unit is equipped with a CO2 return pipeline, which is used to transport part of the removed CO2 to the free plate area of ​​the bubbling fluidized bed gasifier.

2. The system for preparing SAF syngas based on bubbling fluidized bed biomass gasification according to claim 1, characterized in that, The bubbling fluidized bed gasifier includes a gasifier body, which has a free plate zone, a reaction bed, an air distribution zone and a slag discharge section arranged from top to bottom inside. A syngas outlet is provided on the top side of the free plate area, which is connected to the air inlet of the cyclone separator; a gasifying agent inlet is provided on the side wall of the air distribution area. The sidewall of the reaction bed is provided with a sealed pressurized feed port, and the reaction bed is filled with bed material.

3. The system for preparing SAF syngas based on bubbling fluidized bed biomass gasification according to claim 1, characterized in that, The lower part of the cyclone separator is provided with a return leg, and a return valve is provided on the return leg to return the separated solid material to the reaction bed of the bubbling fluidized bed gasifier.

4. The system for preparing SAF syngas based on bubbling fluidized bed biomass gasification according to claim 1, characterized in that, The hot-state catalytic filtration-reforming integrated device includes a gas collection chamber, which contains a ceramic candle filter array. This array consists of multiple regularly arranged ceramic filter elements with catalytic reforming catalysts loaded on their surfaces. One side of the gas collection chamber is provided with an inlet manifold that connects to the outlet of the cyclone separator, and the other side is provided with an outlet manifold; the bottom of the gas collection chamber is provided with an ash hopper, and the ash hopper is provided with a sealed ash discharge valve; the top of the gas collection chamber is provided with a backflush main pipe, which is connected to multiple sets of pulse valves; the pulse valves and the ceramic candle filter array are interlocked with the differential pressure monitor and controller.

5. The system for preparing SAF syngas based on bubbling fluidized bed biomass gasification according to claim 1, characterized in that, The reconfigurable dry deep purification unit includes a waste heat recovery device, a dry purification device, an online monitoring device, and a control device connected in sequence. The dry purification device is a multi-bed sequence with program switching, including at least a COS hydrolysis catalytic bed, a desulfurization bed, a dechlorination bed, an alkali metal / trace metal collection bed, and a fine filtration device; The online monitoring device includes at least sensors for detecting H2S / COS, HCl, NH3, dust / aerosols, light hydrocarbons, and tar indicator signals.

6. The system for preparing SAF syngas based on bubbling fluidized bed biomass gasification according to claim 1, characterized in that, It also includes a pharmaceutical plant organic waste liquid and organic hazardous waste disposal unit, which includes a waste liquid pretreatment and atomizing spray device, a secondary combustion chamber / oxidation furnace, a waste heat recovery device, a quenching device and a flue gas purification device connected in sequence. The flue gas purification device includes an alkali absorption unit, an activated carbon injection unit, and a bag filter or catalytic filtration unit.

7. A method for preparing SAF syngas based on bubbling fluidized bed biomass gasification, characterized in that, Includes the following steps: The pretreated biomass feedstock and gasifying agent are fed into a bubbling fluidized bed gasifier for gasification reaction. In the free plate area of ​​the gasifier, the gasifying agent is injected in a staged pulse manner through the gasifying agent nozzles set on both sides, so that the area forms an alternating oxidation and reforming atmosphere, and a deep reforming reaction is carried out to obtain syngas. Syngas is separated by cyclone separator to obtain crude syngas and solid material; the solid material is returned to the gasifier, and the crude syngas enters the hot catalytic filtration-reforming integrated unit for filtration and catalytic reforming to obtain preliminarily purified syngas; The pre-purified syngas is fed into a reconfigurable dry deep purification unit, and the purification bed sequence is dynamically switched according to the impurity fingerprint monitored online for deep purification. The deeply purified syngas is subjected to water-gas shift reaction and CO2 removal treatment in sequence. By adjusting the amount of CO2 reused and the amount of steam added for the shift reaction in a coordinated manner, the H2 / CO molar ratio in the final syngas is stably adjusted to the target range required for SAF synthesis.

8. The method for preparing SAF syngas based on bubbling fluidized bed biomass gasification according to claim 7, characterized in that, The reaction bed temperature of the bubbling fluidized bed gasifier is 750-900℃, and the temperature of the free plate zone is 800-1000℃. The vaporizing agent includes oxygen, water vapor, and recycled CO2; The gasification equivalence ratio (ER) is 0.15-0.35, and the mass ratio of gasification agent to biomass feedstock is 0.2-1.

2. The pulse period of the graded pulse injection is 2–60 seconds, and the duty cycle is 1%–60%.

9. The method for preparing SAF syngas based on bubbling fluidized bed biomass gasification according to claim 7, characterized in that, The water-gas shift reaction adopts a single-stage or two-stage shift process; When performing Fischer-Tropsch (FT) synthesis, adjust the H2 / CO molar ratio of the synthesis gas to 1.8-2.3; The CO2 removal employs one or more combinations of chemical absorption, physical absorption, membrane separation, or pressure swing adsorption.

10. The method for preparing SAF syngas based on bubbling fluidized bed biomass gasification according to claim 7, characterized in that, When treating organic waste liquid or hazardous waste from pharmaceutical plants, the operating temperature of the secondary combustion chamber / oxidation furnace shall not be lower than 850°C and the flue gas residence time shall not be less than 2 seconds. When handling hazardous waste with high halogen load, the operating temperature shall not be lower than 1100℃ and the residence time shall not be less than 2 seconds. The quenching device rapidly crosses the temperature range of 200-450°C for the flue gas, and in conjunction with the subsequent activated carbon injection and filtration unit, it inhibits the resynthesis of dioxins.

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