WO2022036799A1 - 一种原位成型高比表面积生物炭制备装置与方法 - Google Patents

一种原位成型高比表面积生物炭制备装置与方法 Download PDF

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WO2022036799A1
WO2022036799A1 PCT/CN2020/116195 CN2020116195W WO2022036799A1 WO 2022036799 A1 WO2022036799 A1 WO 2022036799A1 CN 2020116195 W CN2020116195 W CN 2020116195W WO 2022036799 A1 WO2022036799 A1 WO 2022036799A1
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pyrolysis
surface area
specific surface
hot
crushing
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高原
贾永锋
李爱民
王少锋
王欣
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Dalian University of Technology
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Dalian University of Technology
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/3007—Moulding, shaping or extruding
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
    • B01J20/20—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising free carbon; comprising carbon obtained by carbonising processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/3078—Thermal treatment, e.g. calcining or pyrolizing
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09C—RECLAMATION OF CONTAMINATED SOIL
    • B09C1/00—Reclamation of contaminated soil
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09C—RECLAMATION OF CONTAMINATED SOIL
    • B09C1/00—Reclamation of contaminated soil
    • B09C1/10—Reclamation of contaminated soil microbiologically, biologically or by using enzymes
    • C—CHEMISTRY; METALLURGY
    • C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
    • C09K—MATERIALS FOR MISCELLANEOUS APPLICATIONS, NOT PROVIDED FOR ELSEWHERE
    • C09K17/00—Soil-conditioning materials or soil-stabilising materials
    • C09K17/02—Soil-conditioning materials or soil-stabilising materials containing inorganic compounds only
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09C—RECLAMATION OF CONTAMINATED SOIL
    • B09C2101/00—In situ
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel

Definitions

  • the invention belongs to the technical field of carbon material preparation, and in particular relates to an in-situ forming high specific surface area biochar preparation device and method.
  • the first method is to add a binder to extrude the biomass raw materials, and then pyrolyze the formed raw materials;
  • the second method is to first prepare biochar powder, Then add organic binder (phenolic resin, sodium carboxymethyl cellulose, asphalt and polyvinyl alcohol, etc.) or inorganic binder (bentonite, montmorillonite, kaolinite and diatomite, etc.) for extrusion molding.
  • organic binder phenolic resin, sodium carboxymethyl cellulose, asphalt and polyvinyl alcohol, etc.
  • inorganic binder bentonite, montmorillonite, kaolinite and diatomite, etc.
  • the direct addition of the binder to the biochar will destroy the pore structure, reduce the specific surface area, and reduce the active adsorption sites. And both methods need to add additional binder, and both need to be formed and carbonized step by step in two sets of devices.
  • the present invention provides a low temperature, in-situ molding, high specific surface area biochar preparation device and process method.
  • An in-situ molding high specific surface area biochar preparation device comprising a crushing and mixing device, a thermocompression pyrolysis device, a cleaning device, a drying device, a gas-liquid separation device, a heat exchange device, a combustible gas recovery device, a concentration reactor and a water
  • the processing device; the crushing and mixing device, the hot-pressing pyrolysis device, the cleaning device and the drying device are connected in sequence; the hot-pressing pyrolysis device is connected with the gas-liquid separation device, the gas-liquid separation device is connected with the heat exchange device, and the heat exchange device is connected with the combustible gas
  • the recovery device is connected; the cleaning device, the concentration reactor and the water treatment device are connected in sequence; the concentration reactor is connected with the heat exchange device, the concentration reactor is connected with the crushing and mixing device; the crushing and mixing device is connected with the gas-liquid separation device;
  • the pyrolysis oil and gas mixture at the outlet of the pyrolysis device is passed into the gas-liquid separation device, and the solid phase is passed into the cleaning device; the liquid phase tar separated by the gas-liquid separation device is passed into the crushing and mixing device, and the high-temperature combustible gas is passed into the heat exchange device;
  • the pyrolysis gas at the outlet of the heat exchange device is passed into the combustible gas recovery device; the hot air of the heat exchange device is passed into the concentration reactor; the washing liquid of the cleaning device is passed into the concentration reactor, and the evaporative condensed water at the outlet of the concentration reactor is passed into the water treatment reaction
  • the concentrated modifier at the outlet of the concentrated reactor is passed into the crushing and mixing device.
  • the crushing and mixing device is mainly composed of a cutting knife group, a screening module, a stirrer, an atomization module and a conveying system.
  • the hot-pressing pyrolysis device is mainly composed of a temperature control system, a pressure control system, a molding die, a pressing module and a heating module.
  • I Crushing and mixing stage Add biomass to the crushing and mixing device, start the crushing and mixing device, crush the biomass into 100 ⁇ 200 mesh powder by the cutting knife group, then add the modifier, start the atomization module and add water, and then use
  • the agitator fully mixes the biomass with the modifier and sends it to the thermocompression pyrolysis device through the conveying system;
  • Hot-pressing and pyrolysis-to-charcoal stage After the mixture enters the hot-pressed pyrolysis device in step 1, start the temperature control system and pressure control system of the hot-pressed pyrolysis device, and adjust the pressure of hot-pressing and pyrolysis to carbonize and temperature, in this stage, continuous, stepped or interactive pressure heating is used, and the three-phase products of pyrolysis oil, pyrolysis gas and pyrolysis carbon are obtained after heat preservation and pressure keeping;
  • the separation device realizes the separation of liquid-phase tar and high-temperature combustible gas.
  • the liquid-phase tar is circulated to the crushing and mixing device to be mixed with the next batch of biomass.
  • the high-temperature combustible gas enters the heat exchange device in the form of high-temperature pyrolysis gas.
  • the air in the heat exchange device undergoes indirect heat exchange, the hot air after heat exchange is sent to the concentration reactor to provide energy for the evaporation of the washing liquid, and the pyrolysis gas after heat exchange is sent to the combustible gas recovery device for collection;
  • Phase III separation and washing in step II, the solid phase produced by the thermocompression pyrolysis device is cleaned and dried by a cleaning device and a drying device to obtain a formed biochar product.
  • the washing liquid discharged from the cleaning device passes through the concentration reactor, and the high-temperature hot air is The evaporation and concentration of the washing liquid provides energy, the concentrated and concentrated modifier is recycled into the crushing and mixing device, and the remaining evaporated condensed water enters the water treatment device, and is discharged after reaching the standard.
  • the biomass includes industrial by-products containing lignin, cellulose and hemicellulose, agricultural waste and municipal waste, such as sludge, black liquor from papermaking, rice husks, straw, wood scraps, bamboo Crumbs, leaves, prolifera, etc., can be one of them, or a mixture of many.
  • the modifier is a mixture of one or more of modifiers such as phosphate ester, pyrophosphoric acid, ammonium polyphosphate, phosphoramide, triammonium phosphate, etc.; the modifier and biomass mass ratio is 0.05 ⁇ 5.
  • the heating method can be resistance heating, electromagnetic coil heating, microwave heating, etc.; the pressurizing method can be mechanical driving or hydraulic driving.
  • the pressing strength of the hot pressing-pyrolysis device is 1-200 MPa/cm 2
  • the heating temperature is 300-500 ° C
  • the time for simultaneous hot-pressing and pyrolysis to carbon is 5-120 min
  • the heating rate is 1 ⁇ 20°C/min
  • the pressure increase rate is 1 ⁇ 20 MPa/cm 2 /min.
  • the main components of biomass include lignin, cellulose and hemicellulose.
  • the amorphous lignin softens and melts, and uses forces such as intermolecular hydrogen bonds, intermolecular van der Waals forces and capillary pressure. , through bridging, filling, chiming, chemical reaggregation and mechanical interlocking, etc. to play a bonding role; in the process of high temperature carbonization (300 ⁇ 500 °C), biomass pyrolysis will produce a certain amount of tar, Sticky substances such as oligosaccharides or polycyclic aromatic hydrocarbons.
  • Pore-making mechanism Use the endothermic, covering, suffocating and free radical trapping effects of flame retardant modifiers to reduce the carbonization temperature of biomass pyrolysis, inhibit excessive ablation of biomass, accelerate polycondensation reaction, and create more pore structures , improve product porosity.
  • biochar material to polluted soil is beneficial to slow down the migration of materials caused by scouring effects such as rainwater, and improve the stabilization effect.
  • the production of biochar materials with high specific surface area can provide more active adsorption sites for the passivation of pollutants such as heavy metals, thereby increasing the adsorption capacity per unit volume of the adsorbent and improving the cost performance of the product.
  • Molded biochar with a certain strength is not only easy to transport, but also not easily affected by external forces such as mechanical agitation in the actual process of dosing, and is not fragile and easy to recover.
  • Figure 1 is a schematic diagram of the process of in-situ forming high specific surface area biochar.
  • the rice husk powder is thoroughly mixed with ammonium polyphosphate and then sent to a hot-pressing pyrolysis device.
  • Adjust the temperature control system and pressure system adopt gradient mode for heating and pressurization, set the heating rate to 10 °C/min, the final temperature to 400 °C, the compression strength to be 2 MPa/cm 2 /min, and the final pressure to be designed to be 80 MPa/min. cm 2 , and the final temperature and final pressure residence time was 60 min.
  • the pressure is slowly released, and the solid-phase product is washed and dried to obtain a shaped biochar product.
  • the washing liquid passes through the concentration reactor, and the concentrated modifier is reused in the crushing and mixing device to be mixed with the next batch of E. prolifera powder, and the evaporated condensed water enters the water treatment device, and is discharged after reaching the standard.
  • the oil and gas mixture produced by pyrolysis enters the gas-liquid separation device to separate the liquid-phase viscous products from the gas-phase products, and the liquid-phase viscous products are recycled to the crushing and mixing device to be mixed with the next batch of Enteromorpha powder, and the gas-phase products are in the form of high-temperature pyrolysis gas
  • the high-temperature pyrolysis gas exchanges heat indirectly with the air in the heat exchange device.
  • the hot air after heat exchange is sent to the concentrating reactor to provide energy for the evaporation of the washing liquid, and the pyrolysis gas after heat exchange is collected for use.

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Abstract

一种原位成型高比表面积生物炭制备装置与方法：经过破碎混匀的生物质和改性剂进入到热压热解装置中，同步完成热压成型和热解成炭，解决了目前成型生物炭材料分步多设备繁琐的制备工艺问题；利用木质素低温熔融软化和热解焦油的黏附、桥接、交联和机械互锁等作用实现原位粘结成型，该过程无需外加任何交联剂，生产成本低；利用微量阻燃类改性剂的覆盖和窒息作用降低生物质热解成炭温度、抑制过度烧蚀、并加速缩聚反应，提高产品比表面积和得率，提升产品性价比。

Description

一种原位成型高比表面积生物炭制备装置与方法 技术领域
本发明属于炭材料制备技术领域，具体涉及一种原位成型高比表面积生物炭制备装置与方法。
 背景技术
近些年，矿产资源的开发、化工产品的生产和污水的排放等工业活动造成我国土壤重金属污染加剧。截至到2019年，全国土壤总超标率已高达16%，受污染耕地面积超过1000万公顷。导致土壤污染的主要重金属包括：砷、镉、镍、铅、铜等生物毒性元素。土壤中的污染物通过生态圈循环进入人体会造成各种疾病。常见的土壤修复技术包括物理修复、化学钝化、生物修复和农业生态修复等。其中，利用廉价生物炭材料作为钝化剂施加于污染土壤中不仅可以吸附重金属污染物，降低其生物有效性，还可以改善土壤理化环境，因此备受关注。
然而，低密度粉末状生物炭施加于污染土壤介质中，易受到地表径流或雨水的冲刷而迁移，造成土壤污染范围扩散，因此开展高密度、高强度的成型生物炭材料的研究非常必要。目前常见成型生物炭材料的制备方法主要包括两种：第一种方法是先加入粘结剂将生物质原料挤压成型，再热解已成型原料；第二种方法是先制备生物炭粉，再加入有机粘结剂（酚醛树脂、羧甲基纤维素钠、沥青和聚乙烯醇等）或无机粘结剂（膨润土、蒙脱土、高岭石和硅藻土等）挤压成型。这两种方法均存在一定的局限性：第一种方法粘结剂在炭化或活化过程的高温作用下（<500℃）易失活，使得终产物抗压强度和密度下降，施加过程中易被搅碎；第二种方法粘结剂直接加入到生物炭中会破坏孔径结构、降低比表面积，减少活性吸附位点。且两种方法均需要额外加入粘结剂，均需成型和炭化分步在两套装置中进行。
此外，将生物炭应用于实际重金属等污染物吸附工艺中，单位质量表面活性位点的含量（包括孔径、边缘缺陷、拓扑缺陷及表面官能团等）直接影响材料的性价比。同等条件下，得率和比表面积越高，相对生产成本越低。此外，热解温度的调控也是减少能耗、降低生产成本的重要因素之一。因此，在材料制备过程中，针对如何实现低温、高比表面积和高产率生物炭有效制备的研究也是非常有意义的。
 技术问题
针对上述情况，为克服现有生产工艺的不足，本发明提供了一种低温、原位成型、高比表面积生物炭的制备装置与工艺方法。
 技术解决方案
本发明的技术方案：
一种原位成型高比表面积生物炭制备装置，包括碎混装置、热压热解装置、清洗装置、烘干装置、气液分离装置、换热装置、可燃气回收装置、浓缩反应器和水处理装置；碎混装置、热压热解装置、清洗装置和烘干装置依次相连；热压热解装置与气液分离装置相连，气液分离装置与换热装置相连，换热装置与可燃气回收装置相连；清洗装置、浓缩反应器和水处理装置依次相连；浓缩反应器与换热装置相连，浓缩反应器与碎混装置相连；碎混装置与气液分离装置相连；
热压热解装置出口的热解油气混合物通入气液分离装置，固相通入清洗装置；气液分离装置分离的液相焦油通入碎混装置中，高温可燃气通入换热装置；换热装置出口的热解气通入可燃气回收装置；换热装置的热空气通入浓缩反应器；清洗装置的水洗液通入浓缩反应器，浓缩反应器出口的蒸发冷凝水通入水处理反应器，浓缩反应器出口的浓缩改性剂通入碎混装置。
所述的碎混装置主要由切削刀组、筛分模块、搅拌器、雾化模块和传送系统组成。
所述的热压热解装置主要由温控系统、压控系统、成型模具、加压模块和加热模块组成。
一种原位成型高比表面积生物炭制备方法，步骤如下：
Ⅰ碎混阶段：将生物质添加到碎混装置中，启动碎混装置，利用切削刀组将生物质破碎成100~200目的粉末，再加入改性剂，启动雾化模块加入水，之后利用搅拌器将生物质与改性剂充分混合后通过传送系统送入热压热解装置；
Ⅱ热压成型热解成炭阶段：待步骤Ⅰ中混合物进入到热压热解装置后，启动热压热解装置的温控系统和压控系统，调节热压成型-热解成炭的压力和温度，此阶段采用连续式、阶梯式或交互式加压加热方式，经过保温和保压后获得的热解油、热解气和热解炭三相产物；热解油气混合物通入气液分离装置，实现液相焦油和高温可燃气分离，液相焦油循环到碎混装置中与下一批生物质混合，高温可燃气以高温热解气的形式进入换热装置，高温热解气与换热装置内的空气进行间接换热，换热后的热空气送入浓缩反应器为水洗液的蒸发提供能量，换热后的热解气送入可燃气回收装置进行收集；
Ⅲ离洗阶段：步骤Ⅱ中热压热解装置产出的固相经清洗装置和烘干装置清洗烘干后获得成型生物炭产品，清洗装置排出的水洗液经过浓缩反应器，高温热空气为水洗液的蒸发浓缩提供能量，浓缩后的浓缩改性剂回用到碎混装置中，剩余蒸发冷凝水进入水处理装置，处理达标后排放。
所述的生物质包括含有木质素、纤维素和半纤维素的工业副产物、农业废弃物及城市废弃物等生物质，例如：污泥、造纸黑液、稻壳、秸秆、木材边角料、竹屑、树叶、浒苔等，可以是其中的一种，也可以是多种混合。
所述的改性剂是磷酸酯、焦磷酸、聚磷酸铵、磷酰胺、磷酸三铵等改性剂的一种或两种以上混合；所述的改性剂与生物质质量比为0.05~5。
所述的加热方式可以是电阻加热、电磁力线圈加热和微波加热等；所述的加压方式可以是机械驱动或液压驱动。
所述的热压-热解装置加压强度为1~200 MPa/cm 2，加热温度为300~500℃，同步热压成型和热解成炭的时间为5~120 min，升温速率为1~20℃/min，升压速率为1~20 MPa/cm 2/min。
本发明的原理：成型机制：生物质主要组成部分包括木质素、纤维素和半纤维素。在低温热压过程中（<300℃），当温度高于木质素玻璃态转化温度后，非晶态的木质素软化熔融，并利用分子间氢键、粒子间范德华力和毛细压力等作用力，通过桥接、充填、嵌合、化学重聚和机械互锁等方式起到粘结作用；在高温成炭过程中（300~500℃），生物质热解会原位产生一定量的焦油、低聚糖或稠环芳烃等粘性物质。在不断加压过程中，这些粘性物质可通过吸附、扩散、缩聚、交联和固化等作用形成具有一定机械强度的成型材料。造孔机制：利用阻燃改性剂的吸热、覆盖、窒息和自由基捕获等作用降低生物质热解过程的成炭温度，抑制生物质过度烧蚀，加速缩聚反应，创造更多孔隙结构，提高产品孔隙度。
 有益效果
本发明的有益效果：
（1）生物炭成型与热解同步实现，简化工艺步骤，减少设备占地，降低生产成本；
（2）热压成型过程中无需外加任何粘结剂，热解成炭过程中无需任何惰性保护气体，大幅度降低生产成本。
（3）高密度成型生物炭材料施加于污染土壤有利于减缓雨水等冲刷作用造成的物料迁移问题，提高稳定化效果。高比表面积生物炭材料的生产可为重金属等污染物的钝化提供更多的活性吸附点位，进而提高吸附剂的单位体积吸附量，提高产品性价比。
（4）具有一定强度成型生物炭不仅便于运输，并且在实际工艺投加过程中不易受到机械搅动等外界力的影响，不易碎，易回收。
 附图说明
图1是原位成型高比表面积生物炭的工艺示意图。
 本发明的实施方式
以下结合附图和技术方案，进一步说明本发明的具体实施方式。
实施例
将1000 g浒苔送入碎混装置中，启动碎混装置，将浒苔破碎成200目的粉末，再加入200 g聚磷酸铵，然后启动雾化模块加入50 g雾化水汽，再启动搅拌器将稻壳粉末与聚磷酸铵充分混合后传送到热压热解装置。调节温控系统和压力系统，升温和加压采用梯度方式，升温速率设置为10℃/min，终温为400℃，加压强度为2 MPa/cm 2/min，终压设计为80 MPa/cm 2，终温和终压停留时间为60 min。热解完成后缓慢卸压，固相产物经过清洗和烘干后获得成型生物炭产品。水洗液经过浓缩反应器，浓缩后的浓缩改性剂回用到碎混装置中与下一批浒苔粉末混合，蒸发冷凝水进入水处理装置，处理达标后排放。热解产生的油气混合物进入气液分离装置将液相粘性产物和气相产物进行分离，液相粘性产物循环到碎混装置中与下一批浒苔粉末混合，气相产物以高温热解气的形式进入换热装置，高温热解气与换热装置内的空气间接换热，换热后的热空气送入浓缩反应器为水洗液的蒸发提供能量，换热后的热解气收集待用。
应该理解，公开实施例的目的在于对本发明进行说明解释，而非是对本发明的限制，一切在本发明的基础上进行简单替换、组合和发展得到的技术方案，都应落入本发明保护范围。

Claims (10)

  1. 一种原位成型高比表面积生物炭制备装置，其特征在于，该原位成型高比表面积生物炭制备装置包括碎混装置、热压热解装置、清洗装置、烘干装置、气液分离装置、换热装置、可燃气回收装置、浓缩反应器和水处理装置；碎混装置、热压热解装置、清洗装置和烘干装置依次相连；热压热解装置与气液分离装置相连，气液分离装置与换热装置相连，换热装置与可燃气回收装置相连；清洗装置、浓缩反应器和水处理装置依次相连；浓缩反应器与换热装置相连，浓缩反应器与碎混装置相连；碎混装置与气液分离装置相连；
    热压热解装置出口的热解油气混合物通入气液分离装置，固相通入清洗装置；气液分离装置分离的液相焦油通入碎混装置中，高温可燃气通入换热装置；换热装置出口的热解气通入可燃气回收装置；换热装置的热空气通入浓缩反应器；清洗装置的水洗液通入浓缩反应器，浓缩反应器出口的蒸发冷凝水通入水处理反应器，浓缩反应器出口的浓缩改性剂通入碎混装置。
  2. 根据权利要求1所述的原位成型高比表面积生物炭制备装置，其特征在于，所述的碎混装置主要由切削刀组、筛分模块、搅拌器、雾化模块和传送系统组成。
  3. 根据权利要求1或2所述的原位成型高比表面积生物炭制备装置，其特征在于，所述的热压热解装置主要由温控系统、压控系统、成型模具、加压模块和加热模块组成。
  4. 一种原位成型高比表面积生物炭制备方法，其特征在于，步骤如下：
    Ⅰ碎混阶段：将生物质添加到碎混装置中，启动碎混装置，利用切削刀组将生物质破碎成100~200目的粉末，再加入改性剂，启动雾化模块加入水，之后利用搅拌器将生物质与改性剂充分混合后通过传送系统送入热压热解装置；
    Ⅱ热压成型热解成炭阶段：待步骤Ⅰ中混合物进入到热压热解装置后，启动热压热解装置的温控系统和压控系统，调节热压成型-热解成炭的压力和温度，此阶段采用连续式、阶梯式或交互式加压加热方式，经过保温和保压后获得的热解油、热解气和热解炭三相产物；热解油气混合物通入气液分离装置，实现液相焦油和高温可燃气分离，液相焦油循环到碎混装置中与下一批生物质混合，高温可燃气以高温热解气的形式进入换热装置，高温热解气与换热装置内的空气进行间接换热，换热后的热空气送入浓缩反应器为水洗液的蒸发提供能量，换热后的热解气送入可燃气回收装置进行收集；
    Ⅲ离洗阶段：步骤Ⅱ中热压热解装置产出的固相经清洗装置和烘干装置清洗烘干后获得成型生物炭产品，清洗装置排出的水洗液经过浓缩反应器，高温热空气为水洗液的蒸发浓缩提供能量，浓缩后的浓缩改性剂回用到碎混装置中，剩余蒸发冷凝水进入水处理装置，处理达标后排放。
  5. 根据权利要求4所述的原位成型高比表面积生物炭制备方法，其特征在于，所述的生物质为含有木质素、纤维素和半纤维素的工业副产物、农业废弃物及城市废弃物中的一种或两种以上混合。
  6. 根据权利要求4或5所述的原位成型高比表面积生物炭制备方法，其特征在于，所述的改性剂是磷酸酯、焦磷酸、聚磷酸铵、磷酰胺、磷酸三铵中一种或两种以上混合；所述的改性剂与生物质质量比为0.05~5。
  7. 根据权利要求4或5所述的原位成型高比表面积生物炭制备方法，其特征在于，所述的加热方式是电阻加热、电磁力线圈加热或微波加热；所述的加压方式是机械驱动或液压驱动。
  8. 根据权利要求6所述的原位成型高比表面积生物炭制备方法，其特征在于，所述的加热方式是电阻加热、电磁力线圈加热或微波加热；所述的加压方式是机械驱动或液压驱动。
  9. 根据权利要求4、5或8所述的原位成型高比表面积生物炭制备方法，其特征在于，所述的热压热解装置的加压强度为1~200 MPa/cm 2，加热温度为300~500℃，同步热压成型和热解成炭的时间为5~120 min，升温速率为1~20℃/min，升压速率为1~20 MPa/cm 2/min。
  10. 根据权利要求6所述的原位成型高比表面积生物炭制备方法，其特征在于，所述的热压热解装置的加压强度为1~200 MPa/cm 2，加热温度为300~500℃，同步热压成型和热解成炭的时间为5~120 min，升温速率为1~20℃/min，升压速率为1~20 MPa/cm 2/min。
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