CN106635112B - A kind of biomass by hydro-thermal liquefaction system and method - Google Patents
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Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/008—Controlling or regulating of liquefaction processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1011—Biomass
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Description
技术领域technical field
本发明涉及生物质能源技术领域，尤其涉及一种生物质水热液化系统及方法。The invention relates to the technical field of biomass energy, in particular to a biomass hydrothermal liquefaction system and method.
背景技术Background technique
生物质水热液化技术是指利用热化学的方法，在有或无催化剂的作用下，在高温高压的液相水热条件下将生物质(比如丝藻、球藻、污泥、花生秸秆、猪粪等)原料转化为生物质油的过程。生物质水热液化技术是一种非常具有发展前景的生物质制油技术，具有许多优势。首先，对比传统的热化学转化技术(如气化和热解)，生物质水热液化技术能够直接将未经干燥的湿生物质转换成能量密集的生物质油，从而避免了干燥过程附加的高能量消耗，因此具有更低的能量消耗率，特别适合处理生物质等湿生物质。其次，生物质水热液化技术不仅可以将生物质中的油脂转化成生物质油，还可将生物质含有的蛋白质和糖类物质也转化为高热值的生物质油。同时生物质具有较高的生长速率、生长环境不占用耕地、较高的脂质含量，能够产生巨大的环境和经济效益。因此，以生物质为原料的生物质液体燃料生产技术具备经济技术可行性，已成为该领域主要的发展趋势之一，它对于缓解环境污染，提高能源安全具有重要意义。Biomass hydrothermal liquefaction technology refers to the use of thermochemical methods to convert biomass (such as silk algae, coccus, sludge, peanut straw, Pig manure, etc.) raw materials into the process of biomass oil. Biomass hydrothermal liquefaction technology is a promising biomass oil production technology with many advantages. First, compared with traditional thermochemical conversion technologies (such as gasification and pyrolysis), biomass hydrothermal liquefaction technology can directly convert undried wet biomass into energy-dense biomass oil, thus avoiding the additional cost of drying process. High energy consumption, so it has a lower energy consumption rate, especially suitable for processing wet biomass such as biomass. Secondly, biomass hydrothermal liquefaction technology can not only convert the oil in biomass into biomass oil, but also convert the protein and sugar contained in biomass into biomass oil with high calorific value. At the same time, biomass has a high growth rate, a growth environment that does not occupy arable land, and a high lipid content, which can produce huge environmental and economic benefits. Therefore, the production technology of biomass liquid fuel with biomass as raw material is economically and technically feasible, and has become one of the main development trends in this field. It is of great significance for alleviating environmental pollution and improving energy security.
但是，在生物质液化反应过程中，由于反应器内的反应温度和反应压力通常在连续进料和连续出料过程中难以保持在液化反应的要求范围(即温度要求为200～400℃，压力要求为5～25Mpa)内，因此现有技术中生物质液化反应系统难以实现连续进料和连续出料的连续式反应，由此不利于生物质水热液化的规模化生产。However, in the process of biomass liquefaction reaction, because the reaction temperature and reaction pressure in the reactor are usually difficult to maintain in the required range of liquefaction reaction during the continuous feeding and continuous discharging process (that is, the temperature requirement is 200-400 °C, the pressure The requirement is within 5-25Mpa), so the biomass liquefaction reaction system in the prior art is difficult to realize the continuous reaction of continuous feeding and continuous discharging, which is not conducive to the large-scale production of biomass hydrothermal liquefaction.
发明内容Contents of the invention
本发明提供一种生物质水热液化系统及方法，能够在生物质液化反应过程中将反应器内的反应温度和反应压力保持于液化反应要求范围内，以使液化反应能够连续进料和连续出料，以利于生物质水热液化的规模化生产。The invention provides a biomass hydrothermal liquefaction system and method, which can keep the reaction temperature and reaction pressure in the reactor within the range required by the liquefaction reaction during the biomass liquefaction reaction, so that the liquefaction reaction can continuously feed and continuously The material is discharged to facilitate the large-scale production of biomass hydrothermal liquefaction.
为达到上述目的，本发明的实施例采用如下技术方案：In order to achieve the above object, embodiments of the present invention adopt the following technical solutions:
一方面，本发明提供了一种生物质水热液化系统，包括：反应器，所述反应器用于进行液化反应，所述反应器连接有进料管和产物排出管，所述进料管上串接有加压装置；产物收集器，所述产物收集器与所述产物排出管的排出端密闭连接；流量控制结构，所述流量控制结构设置于所述产物收集器与所述反应器之间，并用于控制所述产物由所述产物排出管排出至所述产物收集器的流量，以使所述产物排出管的排料流量与所述进料管的进料流量相等。In one aspect, the present invention provides a biomass hydrothermal liquefaction system, comprising: a reactor, the reactor is used for liquefaction reaction, the reactor is connected with a feed pipe and a product discharge pipe, the feed pipe is connected with A pressurizing device is connected in series; a product collector, the product collector is airtightly connected with the discharge end of the product discharge pipe; a flow control structure, the flow control structure is arranged between the product collector and the reactor and used to control the flow rate of the product discharged from the product discharge pipe to the product collector, so that the discharge flow rate of the product discharge pipe is equal to the feed flow rate of the feed pipe.
另一方面，本发明提供了一种生物质水热液化方法，所述方法包括：In another aspect, the present invention provides a biomass hydrothermal liquefaction method, said method comprising:
S1、通过进料管和加压装置向反应器内压入含水的预热物料，并使得所述预热物料内的水在所述反应器内受热气化膨胀，以增大所述反应器内的温度和压力，同时通过产物排出管排出预热产物；S1. Press the water-containing preheated material into the reactor through the feed pipe and the pressurizing device, and make the water in the preheated material gasify and expand when heated in the reactor, so as to enlarge the reactor The temperature and pressure inside, while discharging the preheated product through the product discharge pipe;
S2、当所述反应器内的温度增大至第二预设范围，压力增大至第一预设范围内时，将所述预热物料更换为反应物料，并通过所述进料管和所述加压装置将所述反应物料压入所述反应器内，以使所述反应物料在所述反应器内产生液化反应生成水热液化产物；S2. When the temperature in the reactor increases to the second preset range and the pressure increases to the first preset range, replace the preheated material with the reaction material, and pass through the feed pipe and The pressurizing device presses the reaction material into the reactor, so that the reaction material undergoes a liquefaction reaction in the reactor to generate a hydrothermal liquefaction product;
S3、通过产物排出管将所述水热液化产物排出至产物收集器内，并通过流量控制结构控制所述水热液化产物由所述产物排出管排出至所述产物收集器的流量，以使所述产物排出管的排料流量与所述进料管的进料流量相等。S3. Discharge the hydrothermal liquefaction product into the product collector through the product discharge pipe, and control the flow rate of the hydrothermal liquefaction product discharged from the product discharge pipe to the product collector through the flow control structure, so that The discharge flow of the product discharge pipe is equal to the feed flow of the feed pipe.
本发明提供的一种生物质水热液化系统及方法，在通过进料管和加压装置向反应器内压入含水的预热物料之后，预热物料内的水可在反应器内受热气化膨胀，以将反应器内的温度和压力分别增大至第二预设范围和第一预设范围内，由此通过预热物料预热反应器；之后，可将预热物料更换为反应物料，并通过进料管和加压装置将反应物料压入反应器内，以使反应物料在处于第二预设范围内的温度和处于第一预设范围内的压力环境下产生液化反应，液化反应的产物由产物排出管排出至产物收集器中，并通过流量控制结构控制产物排出管的排料流量，以使产物排出管的排料流量与进料管的进料流量相等，从而将反应器内的温度和压力分别保持于第二预设范围和第一预设范围内。由此，可在通过进料管和加压装置连续向反应器供料，并通过产物排出管连续排出反应器内的物料的同时，将反应器内的温度和压力分别维持于第二预设范围和第一预设范围内，从而可实现生物质水热液化系统的连续式反应，进而有利于生物质水热液化的规模化生产。In the biomass hydrothermal liquefaction system and method provided by the present invention, after the preheated material containing water is pressed into the reactor through the feed pipe and the pressurizing device, the water in the preheated material can be heated by the heated gas in the reactor. expansion to increase the temperature and pressure in the reactor to the second preset range and the first preset range, thereby preheating the reactor by preheating the material; after that, the preheating material can be replaced by the reaction material, and press the reaction material into the reactor through the feed pipe and the pressurizing device, so that the reaction material produces a liquefaction reaction at a temperature within the second preset range and a pressure environment within the first preset range, The product of the liquefaction reaction is discharged from the product discharge pipe into the product collector, and the discharge flow of the product discharge pipe is controlled through the flow control structure, so that the discharge flow of the product discharge pipe is equal to the feed flow of the feed pipe, so that the The temperature and pressure in the reactor are maintained within the second preset range and the first preset range respectively. Thus, the temperature and pressure in the reactor can be maintained at the second preset temperature and pressure while continuously supplying materials to the reactor through the feed pipe and the pressurizing device, and continuously discharging the materials in the reactor through the product discharge pipe. range and the first preset range, so that the continuous reaction of the biomass hydrothermal liquefaction system can be realized, which is beneficial to the large-scale production of the biomass hydrothermal liquefaction.
附图说明Description of drawings
为了更清楚地说明本发明实施例或现有技术中的技术方案，下面将对实施例或现有技术描述中所需要使用的附图作简单地介绍，显而易见地，下面描述中的附图仅仅是本发明的一些实施例，对于本领域普通技术人员来讲，在不付出创造性劳动的前提下，还可以根据这些附图获得其他的附图。In order to more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the following will briefly introduce the drawings that need to be used in the description of the embodiments or the prior art. Obviously, the accompanying drawings in the following description are only These are some embodiments of the present invention. Those skilled in the art can also obtain other drawings based on these drawings without creative work.
图1为本发明实施例生物质水热液化系统的第一种结构示意图；Fig. 1 is the first structural schematic diagram of the biomass hydrothermal liquefaction system of the embodiment of the present invention;
图2为本发明实施例生物质水热液化系统的第二种结构示意图；Fig. 2 is the second structural schematic diagram of the biomass hydrothermal liquefaction system of the embodiment of the present invention;
图3为本发明实施例生物质水热液化系统中流量调节阀的结构示意图；3 is a schematic structural view of a flow regulating valve in a biomass hydrothermal liquefaction system according to an embodiment of the present invention;
图4为本发明实施例生物质水热液化系统中过滤装置的结构示意图；4 is a schematic structural view of a filtration device in a biomass hydrothermal liquefaction system according to an embodiment of the present invention;
图5为本发明实施例生物质水热液化方法的流程图。Fig. 5 is a flowchart of a biomass hydrothermal liquefaction method according to an embodiment of the present invention.
附图标记：Reference signs:
1－反应器；2－进料管；3－产物排出管；4－加压装置；5－产物收集器；6－流量控制结构；61－壳体；62－流道；63－倒锥型阀口；64－锥型针；65－丝杠；66－手柄；67－产物入口；68－产物出口；7－送气增压装置；8－背压阀；9－萃取液注入结构；10－搅拌结构；11－分液器；12－过滤装置；121－外壳；122－进液口；123－排液口；124－排渣口；125－滤芯；13－溶剂蒸发装置；14－物料储存装置；15－搅拌装置；16－流量脉冲缓冲器；17－碎料装置；18－预热装置；100－第一传送泵；200－第二传送泵。1-reactor; 2-feed pipe; 3-product discharge pipe; 4-pressurizing device; 5-product collector; 6-flow control structure; 61-shell; 62-flow channel; 63-inverted cone Valve port; 64-tapered needle; 65-lead screw; 66-handle; 67-product inlet; 68-product outlet; 7-air booster device; 8-back pressure valve; Stirring structure; 11-liquid separator; 12-filter device; 121-shell; 122-liquid inlet; 123-liquid discharge port; 124-slag discharge port; 125-filter element; 13-solvent evaporation device; device; 15-stirring device; 16-flow pulse buffer; 17-crushing device; 18-preheating device; 100-first transfer pump; 200-second transfer pump.
具体实施方式Detailed ways
下面将结合本发明实施例中的附图，对本发明实施例中的技术方案进行清楚、完整地描述，显然，所描述的实施例仅仅是本发明一部分实施例，而不是全部的实施例。基于本发明中的实施例，本领域普通技术人员在没有做出创造性劳动前提下所获得的所有其他实施例，都属于本发明保护的范围。The following will clearly and completely describe the technical solutions in the embodiments of the present invention with reference to the accompanying drawings in the embodiments of the present invention. Obviously, the described embodiments are only some, not all, embodiments of the present invention. Based on the embodiments of the present invention, all other embodiments obtained by persons of ordinary skill in the art without making creative efforts belong to the protection scope of the present invention.
在本发明的描述中，需要理解的是，术语“中心”、“上”、“下”、“前”、“后”、“左”、“右”、“竖直”、“水平”、“顶”、“底”、“内”、“外”等指示的方位或位置关系为基于附图所示的方位或位置关系，仅是为了便于描述本发明和简化描述，而不是指示或暗示所指的装置或元件必须具有特定的方位、以特定的方位构造和操作，因此不能理解为对本发明的限制。在本发明的描述中，除非另有说明，“多个”的含义是两个或两个以上。In describing the present invention, it is to be understood that the terms "center", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", The orientations or positional relationships indicated by "top", "bottom", "inner", "outer", etc. are based on the orientations or positional relationships shown in the drawings, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying References to devices or elements must have a particular orientation, be constructed, and operate in a particular orientation and therefore should not be construed as limiting the invention. In the description of the present invention, unless otherwise specified, "plurality" means two or more.
参照图1，图1为本发明实施例生物质水热液化系统的一个具体实施例，本实施例的生物质水热液化系统包括：反应器1，所述反应器1用于进行液化反应，所述反应器1连接有进料管2和产物排出管3，所述进料管2上串接有加压装置4；产物收集器5，所述产物收集器5与所述产物排出管3的排出端密闭连接；流量控制结构6，所述流量控制结构6设置于所述产物收集器5与所述反应器1之间，并用于控制所述产物由所述产物排出管3排出至所述产物收集器5的流量，以使所述产物排出管3的排料流量与所述进料管2的进料流量相等。Referring to Fig. 1, Fig. 1 is a specific embodiment of the biomass hydrothermal liquefaction system of the embodiment of the present invention. The biomass hydrothermal liquefaction system of this embodiment includes: a reactor 1, which is used for liquefaction reaction, The reactor 1 is connected with a feed pipe 2 and a product discharge pipe 3, and the feed pipe 2 is connected in series with a pressurizing device 4; a product collector 5, and the product collector 5 is connected with the product discharge pipe 3 The discharge end is airtightly connected; the flow control structure 6, the flow control structure 6 is arranged between the product collector 5 and the reactor 1, and is used to control the discharge of the product from the product discharge pipe 3 to the The flow rate of the product collector 5 is adjusted so that the discharge flow rate of the product discharge pipe 3 is equal to the feed flow rate of the feed pipe 2.
本发明提供的一种生物质水热液化系统，在通过进料管2和加压装置4向反应器1内压入含水的预热物料之后，预热物料内的水可在反应器1内受热气化膨胀，以将反应器1内的温度和压力分别增大至第二预设范围和第一预设范围内，由此通过预热物料预热了反应器1；之后，可将预热物料更换为反应物料，并通过进料管2和加压装置4将反应物料压入反应器1内，以使反应物料在处于第二预设范围内的温度和处于第一预设范围内的压力环境下产生液化反应，液化反应的产物由产物排出管3排出至产物收集器5中，并通过流量控制结构6控制产物排出管3的排料流量，以使产物排出管3的排料流量与进料管2的进料流量相等，从而将反应器1内的温度和压力分别保持于第二预设范围和第一预设范围内。由此，可在通过进料管2和加压装置4连续向反应器1供料，并通过产物排出管3连续排出反应器1内的物料的同时，将反应器1内的温度和压力分别维持于第二预设范围和第一预设范围内，从而可实现生物质水热液化系统的连续式反应，进而有利于生物质水热液化的规模化生产。In the biomass hydrothermal liquefaction system provided by the present invention, after the water-containing preheated material is pressed into the reactor 1 through the feed pipe 2 and the pressurizing device 4, the water in the preheated material can be discharged in the reactor 1 Heated gasification and expansion to increase the temperature and pressure in the reactor 1 to the second preset range and the first preset range respectively, thereby preheating the reactor 1 through the preheated material; after that, the preheated The hot material is replaced by the reaction material, and the reaction material is pressed into the reactor 1 through the feed pipe 2 and the pressurizing device 4, so that the temperature of the reaction material is within the second preset range and within the first preset range The liquefaction reaction occurs under a pressure environment, and the product of the liquefaction reaction is discharged from the product discharge pipe 3 to the product collector 5, and the discharge flow rate of the product discharge pipe 3 is controlled by the flow control structure 6, so that the discharge of the product discharge pipe 3 The flow rate is equal to the feed flow rate of the feed pipe 2, so as to keep the temperature and pressure in the reactor 1 within the second preset range and the first preset range respectively. Thus, while continuously supplying materials to the reactor 1 through the feed pipe 2 and the pressurizing device 4, and continuously discharging the materials in the reactor 1 through the product discharge pipe 3, the temperature and pressure in the reactor 1 can be controlled respectively. Maintaining within the second preset range and the first preset range, the continuous reaction of the biomass hydrothermal liquefaction system can be realized, which is beneficial to the large-scale production of the biomass hydrothermal liquefaction.
需要说明的是，由于当产物排出管3的排料流量大于进料管2的进料流量时，反应器1内的物料存留量减少，因此反应器1内的反应压力降低，同时物料在反应器1内的停留时间变短，物料在反应器1内的加热时间变短，反应器1内的反应温度降低；相反，当产物排出管3的排料流量小于进料管2的进料流量时，反应器1内的物料存留量逐渐升高，因此反应器1内的反应压力增大，同时物料在反应器1内的停留时间变长，物料在反应器1内的加热时间变长，反应器1内的反应温度升高。因此，只有当产物排出管3的排料流量等于进料管2的进料流量时，反应器1内的反应温度和反应压力才能分别保持于第二预设范围内和第一预设范围内。It should be noted that because when the discharge flow rate of the product discharge pipe 3 is greater than the feed flow rate of the feed pipe 2, the amount of material retained in the reactor 1 decreases, so the reaction pressure in the reactor 1 decreases, and the material is reacting simultaneously. The residence time in the reactor 1 is shortened, the heating time of the material in the reactor 1 is shortened, and the reaction temperature in the reactor 1 is reduced; on the contrary, when the discharge flow rate of the product discharge pipe 3 is less than the feed flow rate of the feed pipe 2 , the material retention in the reactor 1 increases gradually, so the reaction pressure in the reactor 1 increases, and the residence time of the material in the reactor 1 becomes longer simultaneously, and the heating time of the material in the reactor 1 becomes longer. The reaction temperature in the reactor 1 rises. Therefore, only when the discharge flow rate of the product discharge pipe 3 is equal to the feed flow rate of the feed pipe 2, the reaction temperature and reaction pressure in the reactor 1 can be maintained in the second preset range and the first preset range respectively .
其中，预热物料可以为水，也可以为生物质和水组成的混合物，在此不做具体限定。反应物料为生物质和水组成的混合物。Wherein, the preheating material may be water, or a mixture of biomass and water, which is not specifically limited here. The reaction material is a mixture of biomass and water.
另外，需要说明的是，第一预设范围为反应器1内反应物料能够进行液化反应所需的压力范围，第二预设范围为反应器1内反应物料能够进行液化反应所需的温度范围。In addition, it should be noted that the first preset range is the pressure range required for the liquefaction reaction of the reaction materials in the reactor 1, and the second preset range is the temperature range required for the liquefaction reaction of the reaction materials in the reactor 1. .
再者，为了能够通过产物收集器5连续地接收产物，优选产物收集器5为多个，当多个产物收集器5中的一个在用于收集由产物排出管3排出的产物时，可采用其他的产物收集器5进行产物的萃取或分离等操作，由此通过产物收集器5可实现产物的连续接收。其中，产物收集器5的数量可以为两个、三个或四个等等，在此不做具体限定。Furthermore, in order to be able to continuously receive the product by the product collector 5, preferably there are multiple product collectors 5, and when one of the multiple product collectors 5 is used to collect the product discharged by the product discharge pipe 3, it can be used Other product collectors 5 perform operations such as extraction or separation of products, so that the continuous reception of products can be realized through the product collector 5 . Wherein, the number of product collectors 5 may be two, three or four, etc., which is not specifically limited here.
在图1所示的实施例中，反应器1可以为管式反应器，也可以为釜式反应器，在此不做具体限定。In the embodiment shown in FIG. 1 , the reactor 1 may be a tubular reactor or a tank reactor, which is not specifically limited here.
在图1所示的实施例中，加压装置4用于将物料沿进料2压入反应器1内，优选，加压装置4为高压柱塞泵，高压柱塞泵的动力强，且便于控制计算反应物的压入量。In the embodiment shown in Figure 1, the pressurizing device 4 is used to press the material into the reactor 1 along the feed 2, preferably, the pressurizing device 4 is a high-pressure plunger pump, and the power of the high-pressure plunger pump is strong, and It is convenient to control and calculate the pressing amount of reactants.
为了控制产物由产物排出管3排出至产物收集器5的流量，流量控制结构6具体可以包括串接于产物排出管3中的流量调节阀，通过调节流量调节阀的开度即可控制产物沿产物排出管3排出至产物收集器5的流量，以使产物排出管3的排料流量与进料管2的进料流量相等。In order to control the flow rate of the product discharged from the product discharge pipe 3 to the product collector 5, the flow control structure 6 may specifically include a flow regulating valve connected in series in the product discharge pipe 3. By adjusting the opening of the flow regulating valve, the product can be controlled along the The discharge flow rate of the product discharge pipe 3 to the product collector 5 is such that the discharge flow rate of the product discharge pipe 3 is equal to the feed flow rate of the feed pipe 2 .
其中，对流量调节阀的具体结构不做限定，只要能够通过流量调节阀实现产物排出管3排料流量的调节即可。示例的，流量调节阀可以制作为图3所示结构，即，流量调节阀包括壳体61，壳体61上设有产物入口67和产物出口68，壳体61内、产物入口67与产物出口68之间形成有流道62，流道62中设有倒锥型阀口63，还包括锥型针64，锥型针64的直径较小端配合穿设于倒锥型阀口63内，锥型针64的直径较大端连接有丝杠65，丝杠65伸出壳体61外，且丝杠65的中轴线与锥型针64的中轴线共线，壳体61上对应丝杠65的位置开设有与丝杠65上螺纹配合的螺纹孔，丝杠65伸出壳体61外的一端连接有手柄66，通过手柄66旋转丝杠即可调节阀口63的开度，由此调节了流量调节阀的开度。Wherein, the specific structure of the flow regulating valve is not limited, as long as the discharge flow of the product discharge pipe 3 can be adjusted through the flow regulating valve. Exemplarily, the flow regulating valve can be made into the structure shown in Figure 3, that is, the flow regulating valve includes a housing 61, and the housing 61 is provided with a product inlet 67 and a product outlet 68, and in the housing 61, the product inlet 67 and the product outlet A flow channel 62 is formed between the 68, and the flow channel 62 is provided with an inverted cone valve port 63, and also includes a tapered needle 64, the smaller diameter end of the tapered needle 64 fits through the inverted cone valve port 63, The larger diameter end of the tapered needle 64 is connected with a leading screw 65, the leading screw 65 stretches out of the housing 61, and the central axis of the leading screw 65 is collinear with the central axis of the tapered needle 64, and the corresponding leading screw on the housing 61 The position of 65 is provided with the threaded hole that matches with the thread on the lead screw 65, and the end of the lead screw 65 protruding out of the housing 61 is connected with a handle 66, and the opening of the valve port 63 can be adjusted by rotating the lead screw through the handle 66, thus The opening of the flow regulating valve is adjusted.
另外，流量调节阀可以通过手动操作进行调节，也可以通过自动控制进行调节，在此不做具体限定。但是，由于相比于手动调节，自动调节的调节精度和准确性通常较高，因此优选流量调节阀通过自动控制进行自动调节，具体的，为了实现流量调节阀的开度的自动调节，可以包括以下两种具体的实现方式：In addition, the flow regulating valve can be adjusted by manual operation or by automatic control, which is not specifically limited here. However, compared with manual adjustment, the adjustment precision and accuracy of automatic adjustment are usually higher, so it is preferred that the flow adjustment valve is automatically adjusted through automatic control. Specifically, in order to realize the automatic adjustment of the opening of the flow adjustment valve, it may include The following two specific implementation methods:
第一种实现方式：流量控制结构6还包括压力检测单元(图中未示出)和第一控制单元(图中未示出)，压力检测单元位于反应器1内，并用于检测反应器1内的反应压力，第一控制单元用于根据压力检测单元检测到的压力值，控制调节流量调节阀的开度。The first implementation mode: the flow control structure 6 also includes a pressure detection unit (not shown in the figure) and a first control unit (not shown in the figure), the pressure detection unit is located in the reactor 1, and is used to detect the pressure of the reactor 1 The first control unit is used to control and adjust the opening of the flow regulating valve according to the pressure value detected by the pressure detection unit.
具体的，第一控制单元的控制调节过程可以为：当压力检测单元检测到反应器1内的反应压力值小于第一预设范围内的最小值时，第一控制单元控制调小流量调节阀的开度，以增大反应器1内的反应压力；当压力检测单元检测到反应器1内的反应压力值大于第一预设范围内的最大值时，第一控制单元控制调大流量调节阀的开度，以减小反应器1内的反应压力。Specifically, the control and adjustment process of the first control unit may be: when the pressure detection unit detects that the reaction pressure value in the reactor 1 is less than the minimum value within the first preset range, the first control unit controls to reduce the flow regulating valve to increase the reaction pressure in the reactor 1; when the pressure detection unit detects that the reaction pressure value in the reactor 1 is greater than the maximum value in the first preset range, the first control unit controls to increase the flow adjustment Valve opening to reduce the reaction pressure in Reactor 1.
第二种实现方式：流量控制结构6还包括第一流量检测单元(图中未示出)、第二流量检测单元(图中未示出)和第二控制单元(图中未示出)，第一流量检测单元用于检测进料管2的进料流量，第二流量检测单元用于检测流量调节阀的出口流量，当第二流量检测单元检测得到的流量值与第一流量检测单元检测得到的流量值不相等时，第二控制单元控制调节流量调节阀的开度。Second implementation: the flow control structure 6 also includes a first flow detection unit (not shown in the figure), a second flow detection unit (not shown in the figure) and a second control unit (not shown in the figure), The first flow detection unit is used to detect the feed flow of the feed pipe 2, and the second flow detection unit is used to detect the outlet flow of the flow regulating valve. When the flow value detected by the second flow detection unit is the same as that detected by the first flow detection unit When the obtained flow values are not equal, the second control unit controls and adjusts the opening degree of the flow regulating valve.
具体的，第二控制单元的控制调节过程可以为：当第二流量检测单元检测得到的流量值小于第一流量检测单元检测得到的流量值时，第二控制单元控制调大流量调节阀的开度；当第二流量检测单元检测得到的流量值大于第一流量检测单元检测得到的流量值时，第二控制单元控制调小流量调节阀的开度。由此使产物排出管3的排料流量与进料管2的进料流量相等。Specifically, the control and adjustment process of the second control unit may be: when the flow value detected by the second flow detection unit is smaller than the flow value detected by the first flow detection unit, the second control unit controls to increase the opening of the flow regulating valve. degree; when the flow value detected by the second flow detection unit is greater than the flow value detected by the first flow detection unit, the second control unit controls to reduce the opening of the flow regulating valve. This equalizes the discharge flow of the product discharge line 3 to the feed flow of the feed line 2 .
进一步的，为了在液化反应过程中保持反应器1内的反应压力，优选的，如图2所示，生物质水热液化系统还包括与产物收集器5连接的送气增压装置7以及设置于产物收集器5上的背压阀8，送气增压装置7用于在产物收集器5与产物排出管3的排出端连接之前，向产物收集器5内输送气体，以使产物收集器5内的压力增大至与反应器1内的压力相等，背压阀8的压力可调节至与反应器1内的压力相等。由此，可在产物收集器5与产物排出管3的排出端连接之前，调节背压阀8的压力，以使背压阀8的压力与反应器1内的压力相等，并通过送气增压装置7向产物收集器5内输送气体，以使产物收集器5内的压力与反应器1内的压力相等，此时，在将产物排出管3的排出端与此产物收集器5连通之后，产物收集器5内的压力始终与反应器1内的反应压力平衡，由此在液化反应过程中保持了反应器1内的反应压力。Further, in order to maintain the reaction pressure in the reactor 1 during the liquefaction reaction, preferably, as shown in FIG. The back pressure valve 8 on the product collector 5 and the air supply booster 7 are used to deliver gas to the product collector 5 before the product collector 5 is connected with the discharge end of the product discharge pipe 3, so that the product collector 5 The pressure is increased to be equal to the pressure in the reactor 1, and the pressure of the back pressure valve 8 can be adjusted to be equal to the pressure in the reactor 1. Thus, before the product collector 5 is connected to the discharge end of the product discharge pipe 3, the pressure of the back pressure valve 8 can be adjusted so that the pressure of the back pressure valve 8 is equal to the pressure in the reactor 1, and the pressure of the back pressure valve 8 can be increased by feeding air. Device 7 delivers gas in the product collector 5, so that the pressure in the product collector 5 is equal to the pressure in the reactor 1. At this time, after the discharge end of the product discharge pipe 3 is communicated with this product collector 5, The pressure in the product collector 5 is always balanced with the reaction pressure in the reactor 1, thereby maintaining the reaction pressure in the reactor 1 during the liquefaction reaction.
其中，为了防止送气增压装置7向产物收集器5内输送的气体与液化反应的产物之间产生化学反应，优选送气增压装置7向产物收集器5内输送的气体为活性较低的气体或惰性气体。进一步的，优选，此气体为氮气，氮气为自然界中广泛存在的低活性气体，因此容易实现，且成本较低。Wherein, in order to prevent chemical reaction between the gas transported by the air supply booster device 7 into the product collector 5 and the product of the liquefaction reaction, the gas delivered by the gas supply booster device 7 to the product collector 5 is preferably a gas with lower activity or inert gas. Further, preferably, the gas is nitrogen, which is a low-activity gas that widely exists in nature, so it is easy to implement and the cost is low.
另外，产物收集器5上还设有泄压阀(图中未示出)，泄压阀用于将产物收集器5内压力降为常压。In addition, the product collector 5 is also provided with a pressure relief valve (not shown in the figure), and the pressure relief valve is used to reduce the pressure in the product collector 5 to normal pressure.
具体的，送气增压装置7可以制作为如图2所示的结构，即，送气增压装置包括气源、送气管以及串接于送气管中的送气泵，送气管连接于气源与产物收集器5之间，送气泵用于将气源中的气体沿送气管压入产物收集器5内。Specifically, the air supply and booster device 7 can be made into a structure as shown in Figure 2, that is, the air supply and booster device includes an air source, an air supply pipe, and an air supply pump connected in series in the air supply pipe, and the air supply pipe is connected between the gas source and the product. Between the collectors 5, the air supply pump is used to press the gas in the gas source into the product collector 5 along the air supply pipe.
在图1所示的实施例中，产物收集器5可以仅作为产物的收集容器，然后再将产物收集容器中的产物通入另外的萃取装置内以萃取出固相料渣中包裹的生物油，产物收集器5也可以作为萃取装置的容器以用于生物油的萃取，在此不做具体限定。但是，为了减少生物质水热液化系统所包括的零部件的数量，以节省成本，优选采用上述第二种方案，即，产物收集器5作为萃取装置的容器以用于生物油的萃取，具体的，如图2所示，产物收集器5包括萃取液注入结构9和搅拌结构10，萃取液注入结构9用于向产物收集器5内注入萃取液，搅拌结构10用于搅拌产物收集器5内的产物和萃取液，以使萃取液溶出产物中的生物油，由此可通过连接有萃取液注入结构9和搅拌结构10的产物收集器5实现生物油的萃取，在萃取完成后，可静置产物收集器5中的产物和萃取液，以使产物中的固相料渣沉降，并与由水、溶解有生物油的萃取液组成的液相产物分层，以获得固相料渣和由水、溶解有生物油的萃取液组成的液相产物，其中，位于下层的固相料渣可由f通道排出。In the embodiment shown in Figure 1, the product collector 5 can only be used as a collection container for the product, and then the product in the product collection container is passed into another extraction device to extract the bio-oil wrapped in the solid phase residue , the product collector 5 can also be used as a container of the extraction device for the extraction of bio-oil, which is not specifically limited here. However, in order to reduce the number of components included in the biomass hydrothermal liquefaction system and save costs, it is preferable to adopt the second solution above, that is, the product collector 5 is used as a container of the extraction device for the extraction of bio-oil, specifically Yes, as shown in Figure 2, the product collector 5 includes an extract liquid injection structure 9 and a stirring structure 10, the extract liquid injection structure 9 is used to inject the extract liquid into the product collector 5, and the stirring structure 10 is used to stir the product collector 5 The product and the extract in the extract, so that the extract dissolves the bio-oil in the product, thus the extraction of the bio-oil can be realized through the product collector 5 connected with the extract injection structure 9 and the stirring structure 10, after the extraction is completed, it can be The product and the extract in the product collector 5 are left to stand, so that the solid phase slag in the product settles, and is layered with the liquid phase product composed of water and the extract liquid dissolved with bio-oil to obtain the solid phase slag and a liquid phase product composed of water and bio-oil-dissolved extract, wherein the solid phase slag located in the lower layer can be discharged from the f channel.
进一步的，为了分离液相产物中的水和溶解有生物油的萃取液，以实现资源的合理利用，如图2所示，生物质水热液化系统还包括分液器11，分液器11用于分层分离产物收集器5内的水以及溶解有生物油的萃取液，以分别获得水和溶解有生物油的萃取液，其中，水由h通道排出后，可作为工业用水加以循环利用，而溶解有生物油的萃取液为生物油产品的制取原料，从而实现了资源的合理利用，同时浓缩了生物油混合液。Further, in order to separate the water in the liquid phase product and the extract solution dissolved in bio-oil, so as to realize the rational utilization of resources, as shown in Figure 2, the biomass hydrothermal liquefaction system also includes a separator 11, a separator 11 It is used to separate the water in the product collector 5 and the extract solution dissolved in bio-oil to obtain water and the extract solution dissolved in bio-oil respectively, wherein the water can be recycled as industrial water after being discharged from the h channel , and the extract solution dissolved with bio-oil is the raw material for producing bio-oil products, thereby realizing the rational utilization of resources and concentrating the bio-oil mixture.
在将产物收集器5中的液相产物通入分液器之前，为了去除液相产物中残留的固相料渣，以避免残留的固相料渣污染或堵塞分液器，优选的，如图2所示，生物质水热液化系统还包括过滤装置12，过滤装置12用于在将产物收集器5内的水以及溶解有生物油的萃取液通入分液器11之前，滤除水以及溶解有生物油的萃取液中残留的固相料渣，以防止固相料渣进入分液器内而造成污染或堵塞。其中，产物收集器5内的水以及溶解有生物油的萃取液可通过第一传送泵100泵入过滤装置12内，另外，过滤装置12所滤除的固相料渣可由g通道排出。Before the liquid phase product in the product collector 5 is passed into the separator, in order to remove the residual solid phase slag in the liquid phase product, in order to avoid the residual solid phase material slag from polluting or blocking the liquid separator, preferably, such as As shown in Figure 2, the biomass hydrothermal liquefaction system also includes a filter device 12, which is used to filter out water before passing the water in the product collector 5 and the extract liquid dissolved with bio-oil into the liquid separator 11 And the residual solid phase slag in the bio-oil-dissolved extract to prevent the solid phase slag from entering the liquid separator and causing pollution or blockage. Wherein, the water in the product collector 5 and the extract solution dissolved in bio-oil can be pumped into the filter device 12 through the first delivery pump 100, and the solid phase residue filtered by the filter device 12 can be discharged through the g channel.
其中，过滤装置12的具体结构可以制作为如图4所示结构，即，过滤装置12包括外壳121，外壳121的顶部设有进液口122，进液口122与产物收集器5连通，外壳121的底部设有排液口123和排渣口124，外壳121内设有滤芯125，滤芯125的出口与排液口123连通。Wherein, the concrete structure of filtering device 12 can be made as structure as shown in Figure 4, that is, filtering device 12 comprises shell 121, and the top of shell 121 is provided with liquid inlet 122, and liquid inlet 122 communicates with product collector 5, and shell The bottom of 121 is provided with a liquid discharge port 123 and a slag discharge port 124 , and a filter element 125 is provided inside the housing 121 , and the outlet of the filter element 125 communicates with the liquid discharge port 123 .
为了防止固相料渣堵塞滤芯125入口，优选的，滤芯125的入口位于排渣口124的上方，由此防止了固相料渣堵塞滤芯125的入口。In order to prevent the solid-phase slag from blocking the inlet of the filter element 125 , preferably, the inlet of the filter element 125 is located above the slag outlet 124 , thereby preventing the solid-phase slag from blocking the inlet of the filter element 125 .
进一步的，为了去除溶解有生物油的萃取液中的溶剂和残留的水，以获得生物油产品，优选的，如图2所示，生物质水热液化系统还包括溶剂蒸发装置13，溶剂蒸发装置13用于蒸发去除分液器11分离得到的溶解有生物油的萃取液中的萃取液和残留的水，以获得生物油。其中，分液器11分离得到的溶解有生物油的萃取液可通过第二传送泵200泵入溶剂蒸发装置13内，且溶剂蒸发装置13所采用的热介质由j通道通入溶剂蒸发装置13内，并由k通道排出溶剂蒸发装置13，蒸发出的水和萃取液由i通道排出，生物油产品由l通道排出。Further, in order to remove the solvent and residual water in the extract dissolved with bio-oil to obtain bio-oil products, preferably, as shown in Figure 2, the biomass hydrothermal liquefaction system also includes a solvent evaporation device 13, and the solvent evaporates The device 13 is used to evaporate and remove the extract and residual water in the bio-oil-dissolved extract separated by the liquid separator 11 to obtain bio-oil. Wherein, the bio-oil-dissolved extract separated by the separator 11 can be pumped into the solvent evaporator 13 through the second delivery pump 200, and the heat medium used by the solvent evaporator 13 is passed into the solvent evaporator 13 through the j channel The solvent evaporation device 13 is discharged from channel k, the evaporated water and extract are discharged from channel i, and the bio-oil product is discharged from channel l.
在图1所示的实施例中，为了便于向反应器1内提供反应物料，优选的，如图2所示，还包括物料储存装置14，物料储存装置14内储存有反应物料，物料储存装置14连接于进料管2的入口端，用于向进料管2提供反应物料。In the embodiment shown in Fig. 1, in order to provide reaction material in reactor 1 conveniently, preferably, as shown in Fig. 2, also comprise material storage device 14, store reaction material in material storage device 14, material storage device 14 is connected to the inlet end of the feed pipe 2 for providing the feed pipe 2 with reaction materials.
其中，为了防止反应物料在物料储存装置14内因长时间静置而产生分层，从而导致进入反应器1内的反应物料浓度不均，优选的，如图2所示，物料储存装置14内设有搅拌装置15，搅拌装置15用于在供液过程中搅拌物料储存装置14内的反应物料，以防止反应物料产生静置分层。Wherein, in order to prevent the reaction materials from stratifying due to standing still for a long time in the material storage device 14, resulting in uneven concentration of the reaction materials entering the reactor 1, preferably, as shown in Figure 2, the material storage device 14 is equipped with There is a stirring device 15, which is used to stir the reaction materials in the material storage device 14 during the liquid supply process, so as to prevent the reaction materials from standing and stratifying.
在图1所示的实施例中，为了减小加压装置2的输出流量脉冲，优选的，如图2所示，生物质水热液化系统还包括流量脉冲缓冲器16，流量脉冲缓冲器16包括囊状容器(图中未示出)以及罩设于囊状容器外的壳体(图中未示出)，囊状容器串接于加压装置4和反应器1之间的进料管2上，囊状容器由弹性可伸缩材料制作，壳体由刚性材料制作，囊状容器膨胀后的最大容积大于壳体的容积，且囊状容器在处于收缩状态时与壳体内壁之间具有间隙。由此加压装置4排出的反应物料可缓存至囊状容器内，并在囊状容器弹性收缩力的作用下逐渐排出至反应器1内，由此降低了加压装置4的输出流量脉冲。In the embodiment shown in Figure 1, in order to reduce the output flow pulse of the pressurizing device 2, preferably, as shown in Figure 2, the biomass hydrothermal liquefaction system further includes a flow pulse buffer 16, a flow pulse buffer 16 Including a bladder container (not shown in the figure) and a casing (not shown in the figure) that is placed outside the bladder container, the bladder container is connected in series with the feed pipe between the pressurizing device 4 and the reactor 1 2. The bladder-shaped container is made of elastic and stretchable material, and the shell is made of rigid material. The maximum volume of the bladder-shaped container after expansion is greater than the volume of the shell, and there is a gap between the bladder-shaped container and the inner wall of the shell when it is in a contracted state. gap. The reaction materials discharged from the pressurizing device 4 can be buffered into the bladder container, and gradually discharged into the reactor 1 under the action of the elastic contraction force of the bladder container, thereby reducing the output flow pulse of the pressurizing device 4 .
进一步的，为了提高反应物料的液化反应效率，优选的，如图2所示，物料储存装置14的入口处连接有碎料装置17，碎料装置17用于在将反应物料储存至物料储存装置14之前，将反应物料粉碎至100目以下，以提高液化反应的效率。Further, in order to improve the liquefaction reaction efficiency of the reaction materials, preferably, as shown in Figure 2, the inlet of the material storage device 14 is connected with a crushing device 17, and the crushing device 17 is used to store the reaction materials in the material storage device Before 14, crush the reaction material to below 100 mesh to improve the efficiency of the liquefaction reaction.
其中，碎料装置17可以为粉碎机或胶体磨等等，在此不做具体限定。Wherein, the crushing device 17 may be a pulverizer or a colloid mill, etc., which are not specifically limited here.
为了降低生物质水热液化系统的运行成本，提高能量利用率，优选的，如图2所示，生物质水热液化系统还包括预热装置18，预热装置18包括外管(图中未示出)以及位于外管内的内管(图中未示出)，外管与内管之间具有间隙通道，内管串接于进料管2中，间隙通道串接于产物排出管3中，或者，内管串接于产物排出管3中，间隙通道串接于进料管2中。由此利用了液化反应后的余热来预热反应前的物料，从而降低了生物质水热液化系统的运行成本，提高了能量利用率。In order to reduce the operating cost of the biomass hydrothermal liquefaction system and improve energy utilization, preferably, as shown in Figure 2, the biomass hydrothermal liquefaction system also includes a preheating device 18, and the preheating device 18 includes an outer pipe (not shown in the figure) shown) and an inner tube (not shown) located in the outer tube, there is a gap channel between the outer tube and the inner tube, the inner tube is connected in series in the feed pipe 2, and the gap channel is connected in series in the product discharge pipe 3 , or, the inner pipe is connected in series in the product discharge pipe 3, and the gap channel is connected in series in the feed pipe 2. Therefore, the waste heat after the liquefaction reaction is used to preheat the material before the reaction, thereby reducing the operating cost of the biomass hydrothermal liquefaction system and improving the energy utilization rate.
在图1或图2所示的实施例中，优选反应器1为磁力搅拌反应釜，磁力搅拌反应釜能够在反应过程中搅拌反应物料，由此可提高反应率，同时避免产物中的固相料渣堵塞反应器1，且磁力搅拌反应釜的密封性能较优，更利于保持反应器1内的反应压力。In the embodiment shown in Fig. 1 or Fig. 2, preferably reactor 1 is a magnetically stirred reactor, and the magnetically stirred reactor can stir the reaction materials in the reaction process, thus the reaction rate can be improved, and the solid phase in the product can be avoided simultaneously. The slag blocks the reactor 1, and the sealing performance of the magnetic stirring reactor is better, which is more conducive to maintaining the reaction pressure in the reactor 1.
参见图5，本发明实施例还提供了一种生物质水热液化方法，此方法包括：Referring to Fig. 5, an embodiment of the present invention also provides a biomass hydrothermal liquefaction method, which includes:
S1、通过进料管和加压装置向反应器内压入含水的预热物料，并使得所述预热物料内的水在所述反应器内受热气化膨胀，以增大所述反应器内的温度和压力，同时通过产物排出管排出预热产物；S1. Press the water-containing preheated material into the reactor through the feed pipe and the pressurizing device, and make the water in the preheated material gasify and expand when heated in the reactor, so as to enlarge the reactor The temperature and pressure inside, while discharging the preheated product through the product discharge pipe;
S2、当所述反应器内的温度增大至第二预设范围，压力增大至第一预设范围内时，将所述预热物料更换为反应物料，并通过所述进料管和所述加压装置将所述反应物料压入所述反应器内，以使所述反应物料在所述反应器内产生液化反应生成水热液化产物；S2. When the temperature in the reactor increases to the second preset range and the pressure increases to the first preset range, replace the preheated material with the reaction material, and pass through the feed pipe and The pressurizing device presses the reaction material into the reactor, so that the reaction material undergoes a liquefaction reaction in the reactor to generate a hydrothermal liquefaction product;
S3、通过产物排出管将所述水热液化产物排出至产物收集器内，并通过流量控制结构控制所述水热液化产物由所述产物排出管排出至所述产物收集器的流量，以使所述产物排出管的排料流量与所述进料管的进料流量相等。S3. Discharge the hydrothermal liquefaction product into the product collector through the product discharge pipe, and control the flow rate of the hydrothermal liquefaction product discharged from the product discharge pipe to the product collector through the flow control structure, so that The discharge flow of the product discharge pipe is equal to the feed flow of the feed pipe.
本发明提供的一种生物质水热液化方法，在通过进料管和加压装置向反应器内压入含水的预热物料之后，预热物料内的水可在反应器内受热气化膨胀，以将反应器内的温度和压力分别增大至第二预设范围和第一预设范围内，由此通过预热物料预热了反应器；之后，可将预热物料更换为反应物料，并通过进料管和加压装置将反应物料压入反应器内，以使反应物料在处于第二预设范围内的温度和处于第一预设范围内的压力环境下产生液化反应，液化反应的产物由产物排出管排出至产物收集器中，并通过流量控制结构控制产物排出管的排料流量，以使产物排出管的排料流量与进料管的进料流量相等，从而将反应器内的温度和压力分别保持于第二预设范围和第一预设范围内。由此，可在通过进料管和加压装置连续向反应器供料，并通过产物排出管连续排出反应器内的物料的同时，将反应器内的温度和压力分别维持于第二预设范围和第一预设范围内，从而可实现生物质水热液化系统的连续式反应，进而有利于生物质水热液化的规模化生产。In the hydrothermal liquefaction method of biomass provided by the present invention, after the preheated material containing water is pressed into the reactor through the feed pipe and the pressurizing device, the water in the preheated material can be heated and vaporized and expanded in the reactor , to increase the temperature and pressure in the reactor to the second preset range and the first preset range respectively, thereby preheating the reactor by preheating the material; after that, the preheating material can be replaced with the reaction material , and the reaction material is pressed into the reactor through the feed pipe and the pressurizing device, so that the reaction material produces a liquefaction reaction at a temperature within the second preset range and a pressure environment within the first preset range, and the liquefaction The product of the reaction is discharged from the product discharge pipe into the product collector, and the discharge flow of the product discharge pipe is controlled by the flow control structure, so that the discharge flow of the product discharge pipe is equal to the feed flow of the feed pipe, so that the reaction The temperature and pressure in the device are kept within the second preset range and the first preset range respectively. Thus, the temperature and pressure in the reactor can be maintained at the second preset temperature and pressure while continuously supplying materials to the reactor through the feed pipe and the pressurizing device, and continuously discharging the materials in the reactor through the product discharge pipe. range and the first preset range, so that the continuous reaction of the biomass hydrothermal liquefaction system can be realized, which is beneficial to the large-scale production of the biomass hydrothermal liquefaction.
在上述实施例中，通过流量控制结构控制水热液化产物由物排出管排出至产物收集器的流量具体包括：调节流量调节阀的开度，以控制水热液化产物由产物排出管排出至产物收集器的流量。In the above embodiments, controlling the flow rate of the hydrothermally liquefied product discharged from the product discharge pipe to the product collector through the flow control structure specifically includes: adjusting the opening of the flow regulating valve to control the discharge of the hydrothermally liquefied product from the product discharge pipe to the product collector. Collector traffic.
其中，调节流量调节阀的开度，具体可以包括以下两种不同的操作步骤：Wherein, adjusting the opening degree of the flow regulating valve may specifically include the following two different operation steps:
第一种操作步骤：利用压力检测单元检测反应器内的反应压力；当压力检测单元检测得到的压力值小于第一预设范围内的最小值时，第一控制单元控制调小流量调节阀的开度；当压力检测单元检测得到的压力值大于第一预设范围内的最大值时，第一控制单元控制调大流量调节阀的开度。The first operation step: use the pressure detection unit to detect the reaction pressure in the reactor; when the pressure value detected by the pressure detection unit is less than the minimum value within the first preset range, the first control unit controls to reduce the flow regulating valve. Opening degree: when the pressure value detected by the pressure detection unit is greater than the maximum value within the first preset range, the first control unit controls to increase the opening degree of the flow regulating valve.
第二种操作步骤：利用第一流量检测单元检测进料管的进料流量，并利用第二流量检测单元检测流量调节阀的出口流量；当第二流量检测单元检测得到的流量值小于第一流量检测单元检测得到的流量值时，第二控制单元控制调大流量调节阀的开度；当第二流量检测单元检测得到的流量值大于第一流量检测单元检测得到的流量值时，第二控制单元控制调小流量调节阀的开度。The second operation step: use the first flow detection unit to detect the feed flow of the feed pipe, and use the second flow detection unit to detect the outlet flow of the flow regulating valve; when the flow value detected by the second flow detection unit is less than the first When the flow value detected by the flow detection unit, the second control unit controls to increase the opening of the flow regulating valve; when the flow value detected by the second flow detection unit is greater than the flow value detected by the first flow detection unit, the second The control unit controls to reduce the opening degree of the flow regulating valve.
进一步的，为了在液化反应过程中将反应器内的反应压力始终保持于第一预设范围内，优选的，方法还包括：在产物排出管的排出端与产物收集器连接之前，调节背压阀的压力，使得背压阀的压力位于第一预设范围内，并通过送气增压装置向产物收集器内输送气体，使得产物收集器内的压力位于第一预设范围内，以使反应器内的反应温度和反应压力在产物排出管的排出端与产物收集器连接之后，产物收集器内的压力始终与反应器内的反应压力平衡，由此在液化反应过程中始终将反应器内的反应压力保持于第一预设范围内。Further, in order to keep the reaction pressure in the reactor within the first preset range during the liquefaction reaction, preferably, the method further includes: before the discharge end of the product discharge pipe is connected to the product collector, adjusting the back pressure The pressure of the valve, so that the pressure of the back pressure valve is in the first preset range, and the gas is delivered to the product collector through the air supply booster device, so that the pressure in the product collector is in the first preset range, so that the reaction After the reaction temperature and reaction pressure in the reactor are connected to the product collector at the discharge end of the product discharge pipe, the pressure in the product collector is always balanced with the reaction pressure in the reactor, so that the reaction pressure in the reactor is always maintained during the liquefaction reaction. The reaction pressure is kept within the first preset range.
为了萃取分离产物收集器内的水热液化产物，在步骤S3之后，还包括以下步骤：In order to extract the hydrothermal liquefaction product in the separation product collector, after step S3, the following steps are also included:
S4、通过萃取液注入结构向产物收集器内注入萃取液，并通过搅拌结构搅拌水热液化产物和萃取液5～120min，以使萃取液溶出水热液化产物中的生物油；S4. Inject the extract into the product collector through the extract injection structure, and stir the hydrothermal liquefaction product and the extract for 5 to 120 minutes through the stirring structure, so that the extract dissolves the bio-oil in the hydrothermal liquefaction product;
S5、将产物收集器静置1～3h，使得产物收集器内的固相料渣沉降，并与由水、萃取液和生物油组成的液相产物分层；S5, the product collector is left to stand for 1 to 3 hours, so that the solid phase slag in the product collector settles, and is layered with the liquid phase product composed of water, extract and bio-oil;
S6、将产物收集器内的上清液通入过滤装置内，以滤除上清液中残留的固相料渣，并获得由水和溶解有生物油的萃取液组成的混合液；S6. Passing the supernatant in the product collector into the filter device to filter out the solid phase slag remaining in the supernatant, and obtain a mixed solution composed of water and an extract containing bio-oil;
S7、将混合液通入分液器内，并静置10～60min，使得混合液中的水沉降，并与混合液中溶解有生物油的萃取液分层；S7. Pass the mixed solution into the liquid separator, and let it stand for 10-60 minutes, so that the water in the mixed solution settles, and layer with the extract solution in which the bio-oil is dissolved in the mixed solution;
S8、将溶解有生物油的萃取液通入溶剂蒸发装置内，以蒸发去除溶解有生物油的萃取液中的萃取液和残留的水，并获得生物油。S8. Pass the bio-oil-dissolved extract into a solvent evaporator to evaporate and remove the extract and residual water in the bio-oil-dissolved extract to obtain bio-oil.
为了避免产物收集器的内部高压对萃取液的注入顺畅性产生影响，同时避免产物收集器的内部高温使萃取液挥发，优选的，在步骤S3之后，S4之前，还包括：打开产物收集器的泄压阀，以将产物收集器内的压力降为常压，同时将产物收集器内的温度冷却至30℃左右，以避免产物收集器的内部高压对萃取液的注入顺畅性产生影响，同时避免产物收集器的内部高温使萃取液挥发而影响萃取过程。In order to avoid that the internal high pressure of the product collector has an impact on the smoothness of the injection of the extract, and at the same time avoid the internal high temperature of the product collector from volatilizing the extract, preferably, after step S3 and before S4, it also includes: opening the product collector Pressure relief valve, to reduce the pressure in the product collector to normal pressure, and at the same time cool the temperature in the product collector to about 30°C, so as to avoid the impact of the internal high pressure of the product collector on the smoothness of the injection of the extract, and at the same time Avoid the internal high temperature of the product collector to volatilize the extract and affect the extraction process.
在图5所示的实施例中，步骤S2中的反应物料为由生物质和水组成的混合物，混合物中生物质和水的质量比为0.01～0.3。In the embodiment shown in FIG. 5 , the reaction material in step S2 is a mixture composed of biomass and water, and the mass ratio of biomass to water in the mixture is 0.01˜0.3.
其中，生物质可以为丝藻、球藻、污泥、花生秸秆、猪粪等等，在此不做具体限定，只要能够进行液化反应并生成生物油即可。Among them, the biomass can be silk algae, coccus, sludge, peanut straw, pig manure, etc., which are not specifically limited here, as long as they can undergo liquefaction and generate bio-oil.
结合上述各实施例，以下分别以丝藻、球藻、污泥、花生秸秆、猪粪为例进行液化反应，并生成生物油。In combination with the above-mentioned embodiments, the liquefaction reaction of silk algae, coccus, sludge, peanut straw, and pig manure is carried out below to generate bio-oil.
实施例一：Embodiment one:
以丝藻(藻丝长80cm)为例进行液化反应试验，具体包括以下试验步骤：首先，将丝藻与去离子水按3:17的比例混合均匀，并加入碎料装置以将物料粉碎为粒径小于或等于1mm的浆料进入物料储存装置后备用；然后，通过进料管和高压柱塞泵向管式反应器内通入去离子水，以预热管式反应器，同时通过产物排出管排出预热产物，当管式反应器内的温度达到330℃，压力达到20MPa，开始将去离子水更换为备用的浆料，并打开物料储存装置内的搅拌装置和物料储存装置底部出料口阀门，以将浆料通入高压柱塞泵中，打开高压柱塞泵的出口阀门，以向反应器内通入浆料，同时调节流量调节阀的开度，使系统可连续稳定进出料，其中，高压柱塞泵根据浆料在反应器内预设停留时间3min设计流量，流量大小用公式L＝60V*ρ/t计算，其中L代表流量，V代表反应器的体积，ρ代表浆料在反应条件下密度，t代表浆料在反应器内的停留时间。反应器排出的液化反应产物进入产物收集器中，产物收集器为两个，当其中一个产物收集器内的液化反应产物收集至产物收集器体积的一半后，切换为另一个产物收集器进行收集；在产物收集器内的液化反应产物冷却至30℃左右之后，按比例加入萃取液，同时打开搅拌结构，搅拌30min进行充分萃取后静置1h，使固相料渣充分沉积至产物收集器的底部；然后，关闭过滤装置的排渣口阀门和排液口阀门，打开进液口阀门，并用第一传送泵将有产物收集器内的上清液泵入过滤装置中，然后，打开排液口阀门，使滤液流至分液器中，并在分液器中静置1h充分分层，并通过第二传送泵将分离出的溶解有生物油的萃取液泵入溶剂蒸发装置内；最后，通过溶剂蒸发装置对溶解有生物油的萃取液进行溶剂脱出，剩下的产品即为制得的粗生物油。Taking silk algae (algae filament length 80cm) as an example to carry out the liquefaction test, it specifically includes the following test steps: first, mix the silk algae and deionized water in a ratio of 3:17, and add the crushing device to crush the material into The slurry with a particle size less than or equal to 1mm enters the material storage device and is ready for use; then, feed deionized water into the tubular reactor through the feed pipe and high-pressure plunger pump to preheat the tubular reactor, and at the same time pass the product The discharge pipe discharges the preheated product. When the temperature in the tubular reactor reaches 330°C and the pressure reaches 20MPa, start to replace the deionized water with the spare slurry, and open the stirring device in the material storage device and the outlet at the bottom of the material storage device. The material inlet valve is used to feed the slurry into the high-pressure plunger pump, and the outlet valve of the high-pressure plunger pump is opened to feed the slurry into the reactor, and at the same time adjust the opening of the flow regulating valve so that the system can continuously and stably enter and exit Among them, the high-pressure plunger pump is designed according to the preset residence time of the slurry in the reactor for 3 minutes. The flow rate is calculated by the formula L=60V*ρ/t, where L represents the flow rate, V represents the volume of the reactor, and ρ represents Density of the slurry under reaction conditions, t represents the residence time of the slurry in the reactor. The liquefied reaction product discharged from the reactor enters the product collector, and there are two product collectors. When the liquefied reaction product in one of the product collectors is collected to half the volume of the product collector, switch to another product collector for collection ; After the liquefaction reaction product in the product collector is cooled to about 30°C, add the extract in proportion, and at the same time turn on the stirring structure, stir for 30 minutes to fully extract and then stand still for 1 hour, so that the solid phase slag is fully deposited on the product collector bottom; then, close the slag outlet valve and the liquid outlet valve of the filter device, open the liquid inlet valve, and use the first transfer pump to pump the supernatant in the product collector into the filter device, and then open the drain valve, so that the filtrate flows into the liquid separator, and stand in the liquid separator for 1h to fully stratify, and pump the separated extract solution dissolved in bio-oil into the solvent evaporation device through the second delivery pump; finally , the solvent evaporating device is used to remove the solvent from the bio-oil-dissolved extract, and the remaining product is the obtained crude bio-oil.
试验结表明：丝藻连续液化生成生物油产率在28％，热值在35MJ/kg左右，含氧在15％左右，和间歇液化最佳条件液化产物产率及性质相当。The test results show that the continuous liquefaction of silk algae produces bio-oil with a yield of 28%, a calorific value of about 35MJ/kg, and an oxygen content of about 15%, which are equivalent to the yield and properties of the liquefied product under the best condition of intermittent liquefaction.
实施例二：Embodiment two:
以球藻(直径为3-8um)为例进行液化反应试验，具体包括以下试验步骤：将球藻与去离子水按2:8比例混合均匀形成浆料，并加入物料储存装置以备用；然后，通过进料管和高压柱塞泵向反应器内通入去离子水，以预热反应器，同时通过产物排出管排出预热产物，当反应器内的温度达到330℃，压力达到20MPa，开始将去离子水更换为备用的浆料，并打开物料储存装置内的搅拌装置和物料储存装置底部出料口阀门，以将浆料通入高压柱塞泵中，打开高压柱塞泵的出口阀门，以向反应器内通入浆料，同时调节流量调节阀的开度，使系统可连续稳定进出料，其中，高压柱塞泵根据浆料在反应器内预设停留时间1min设计流量，另外，反应器为无搅拌结构的釜式反应器。反应器排出的液化反应产物进入产物收集器中，产物收集器为两个，当其中一个产物收集器内的液化反应产物收集至产物收集器体积的一半后，切换为另一个产物收集器进行收集；在产物收集器内的液化反应产物冷却至30℃左右之后，按比例加入萃取液，同时打开搅拌结构，搅拌30min进行充分萃取后静置1h，使固相料渣充分沉积至产物收集器的底部；然后，关闭过滤装置的排渣口阀门和排液口阀门，打开进液口阀门，并用第一传送泵将有产物收集器内的上清液泵入过滤装置中，然后，打开排液口阀门，使滤液流至分液器中，并在分液器中静置1h充分分层，并通过第二传送泵将分离出的溶解有生物油的萃取液泵入溶剂蒸发装置内；最后，通过溶剂蒸发装置对溶解有生物油的萃取液进行溶剂脱出，剩下的产品即为制得的粗生物油。The liquefaction test was carried out with coccus (3-8um in diameter) as an example, which specifically included the following test steps: mix coccus and deionized water at a ratio of 2:8 to form a slurry, and add it to the material storage device for standby; then , feed deionized water into the reactor through the feed pipe and high-pressure plunger pump to preheat the reactor, and at the same time discharge the preheated product through the product discharge pipe. When the temperature in the reactor reaches 330°C and the pressure reaches 20MPa, Start to replace deionized water with spare slurry, and open the stirring device in the material storage device and the outlet valve at the bottom of the material storage device to pass the slurry into the high-pressure plunger pump, and open the outlet of the high-pressure plunger pump The valve is used to feed the slurry into the reactor, and at the same time adjust the opening of the flow regulating valve, so that the system can continuously and stably feed and discharge the material. Among them, the high-pressure plunger pump is designed according to the preset residence time of the slurry in the reactor for 1min. In addition, the reactor is a tank reactor with no stirring structure. The liquefied reaction product discharged from the reactor enters the product collector, and there are two product collectors. When the liquefied reaction product in one of the product collectors is collected to half the volume of the product collector, switch to another product collector for collection ; After the liquefaction reaction product in the product collector is cooled to about 30°C, add the extract in proportion, and at the same time turn on the stirring structure, stir for 30 minutes to fully extract and then stand still for 1 hour, so that the solid phase slag is fully deposited on the product collector bottom; then, close the slag outlet valve and the liquid outlet valve of the filter device, open the liquid inlet valve, and use the first transfer pump to pump the supernatant in the product collector into the filter device, and then open the drain valve, so that the filtrate flows into the liquid separator, and stand in the liquid separator for 1h to fully stratify, and pump the separated extract solution dissolved in bio-oil into the solvent evaporation device through the second delivery pump; finally , the solvent evaporating device is used to remove the solvent from the bio-oil-dissolved extract, and the remaining product is the obtained crude bio-oil.
试验结表明：球藻连续液化生成生物油产率在46％，热值在37MJ/kg左右，含氧在9％左右，和间歇液化最佳条件液化产物产率及性质相当。The results of the test show that the yield of bio-oil produced by continuous liquefaction of the algae is 46%, the calorific value is about 37MJ/kg, and the oxygen content is about 9%, which is equivalent to the yield and properties of the liquefied product under the best condition of intermittent liquefaction.
实施例三：Embodiment three:
以污泥为例进行液化反应试验，具体包括以下试验步骤：将污泥浓缩至含水量为85％左右，并加入碎料装置以将物料粉碎为粒径小于或等于1mm的浆料后进入物料储存装置备用；然后，通过进料管和高压柱塞泵向反应器内通入去离子水，以预热反应器，同时通过产物排出管排出预热产物，当反应器内的温度达到330℃，压力达到20MPa，开始将去离子水更换为备用的浆料，并打开物料储存装置内的搅拌装置和物料储存装置底部出料口阀门，以将浆料通入高压柱塞泵中，打开高压柱塞泵的出口阀门，以向反应器内通入浆料，同时调节流量调节阀的开度，使系统可连续稳定进出料，其中，高压柱塞泵根据浆料在反应器内预设停留时间5min设计流量，另外，反应器为全混釜式反应器。反应器排出的液化反应产物进入产物收集器中，产物收集器为两个，当其中一个产物收集器内的液化反应产物收集至产物收集器体积的一半后，切换为另一个产物收集器进行收集；在产物收集器内的液化反应产物冷却至30℃左右之后，按比例加入萃取液，同时打开搅拌结构，搅拌30min进行充分萃取后静置1h，使固相料渣充分沉积至产物收集器的底部；然后，关闭过滤装置的排渣口阀门和排液口阀门，打开进液口阀门，并用第一传送泵将有产物收集器内的上清液泵入过滤装置中，然后，打开排液口阀门，使滤液流至分液器中，并在分液器中静置1h充分分层，并通过第二传送泵将分离出的溶解有生物油的萃取液泵入溶剂蒸发装置内；最后，通过溶剂蒸发装置对溶解有生物油的萃取液进行溶剂脱出，剩下的产品即为制得的粗生物油。Taking sludge as an example to carry out the liquefaction test, it specifically includes the following test steps: Concentrate the sludge to a water content of about 85%, and add a crushing device to crush the material into a slurry with a particle size of less than or equal to 1mm before entering the material The storage device is ready for use; then, pass deionized water into the reactor through the feed pipe and high-pressure plunger pump to preheat the reactor, and at the same time discharge the preheated product through the product discharge pipe, when the temperature in the reactor reaches 330 ° C , the pressure reaches 20MPa, start to replace the deionized water with spare slurry, and open the stirring device in the material storage device and the outlet valve at the bottom of the material storage device to pass the slurry into the high-pressure plunger pump and turn on the high-pressure The outlet valve of the plunger pump is used to feed the slurry into the reactor, and at the same time adjust the opening of the flow regulating valve so that the system can continuously and stably feed and discharge the material. Among them, the high-pressure plunger pump is preset to stay in the reactor according to the slurry. The flow rate is designed for 5 minutes, and the reactor is a fully mixed tank reactor. The liquefied reaction product discharged from the reactor enters the product collector, and there are two product collectors. When the liquefied reaction product in one of the product collectors is collected to half the volume of the product collector, switch to another product collector for collection ; After the liquefaction reaction product in the product collector is cooled to about 30°C, add the extract in proportion, and at the same time turn on the stirring structure, stir for 30 minutes to fully extract and then stand still for 1 hour, so that the solid phase slag is fully deposited on the product collector bottom; then, close the slag outlet valve and the liquid outlet valve of the filter device, open the liquid inlet valve, and use the first transfer pump to pump the supernatant in the product collector into the filter device, and then open the drain valve, so that the filtrate flows into the liquid separator, and stand in the liquid separator for 1h to fully stratify, and pump the separated extract solution dissolved in bio-oil into the solvent evaporation device through the second delivery pump; finally , the solvent evaporating device is used to remove the solvent from the bio-oil-dissolved extract, and the remaining product is the obtained crude bio-oil.
试验结表明：污泥连续液化生成生物油产率在30％，热值在36MJ/kg左右，含氧在13％左右，和间歇液化最佳条件液化产物产率及性质相当。The test results show that the yield of bio-oil produced by continuous sludge liquefaction is 30%, the calorific value is about 36MJ/kg, and the oxygen content is about 13%, which is equivalent to the yield and properties of liquefied products under the best condition of intermittent liquefaction.
实施例四：Embodiment four:
以花生秸秆为例进行液化反应试验，具体包括以下试验步骤：将花生秸秆与去离子水按1:9比例混合均匀，并加入碎料装置以将物料粉碎为粒径小于或等于1mm的浆料后进入物料储存装置以备用；然后，通过进料管和高压柱塞泵向反应器内通入去离子水，以预热反应器，同时通过产物排出管排出预热产物，当反应器内的温度达到330℃，压力达到20MPa，开始将去离子水更换为备用的浆料，并打开物料储存装置内的搅拌装置和物料储存装置底部出料口阀门，以将浆料通入高压柱塞泵中，打开高压柱塞泵的出口阀门，以向反应器内通入浆料，同时调节流量调节阀的开度，使系统可连续稳定进出料，其中，高压柱塞泵根据浆料在反应器内预设停留时间7min设计流量，另外，反应器为管式反应器。反应器排出的液化反应产物进入产物收集器中，产物收集器为两个，当其中一个产物收集器内的液化反应产物收集至产物收集器体积的一半后，切换为另一个产物收集器进行收集；在产物收集器内的液化反应产物冷却至30℃左右之后，按比例加入萃取液，同时打开搅拌结构，搅拌30min进行充分萃取后静置1h，使固相料渣充分沉积至产物收集器的底部；然后，关闭过滤装置的排渣口阀门和排液口阀门，打开进液口阀门，并用第一传送泵将有产物收集器内的上清液泵入过滤装置中，然后，打开排液口阀门，使滤液流至分液器中，并在分液器中静置1h充分分层，并通过第二传送泵将分离出的溶解有生物油的萃取液泵入溶剂蒸发装置内；最后，通过溶剂蒸发装置对溶解有生物油的萃取液进行溶剂脱出，剩下的产品即为制得的粗生物油。Taking peanut straw as an example to carry out the liquefaction test, it specifically includes the following test steps: Mix peanut straw and deionized water at a ratio of 1:9, and add a crushing device to crush the material into a slurry with a particle size of less than or equal to 1mm Finally, it enters the material storage device for standby; then, feeds deionized water into the reactor through the feed pipe and high-pressure plunger pump to preheat the reactor, and at the same time discharges the preheated product through the product discharge pipe. When the temperature reaches 330°C and the pressure reaches 20MPa, start to replace deionized water with spare slurry, and open the stirring device in the material storage device and the outlet valve at the bottom of the material storage device to feed the slurry into the high-pressure plunger pump During the process, open the outlet valve of the high-pressure plunger pump to feed the slurry into the reactor, and at the same time adjust the opening of the flow regulating valve so that the system can continuously and stably feed and discharge the material. The preset residence time is 7min and the design flow rate is designed. In addition, the reactor is a tubular reactor. The liquefied reaction product discharged from the reactor enters the product collector, and there are two product collectors. When the liquefied reaction product in one of the product collectors is collected to half the volume of the product collector, switch to another product collector for collection ; After the liquefaction reaction product in the product collector is cooled to about 30°C, add the extract in proportion, and at the same time turn on the stirring structure, stir for 30 minutes to fully extract and then stand still for 1 hour, so that the solid phase slag is fully deposited on the product collector bottom; then, close the slag outlet valve and the liquid outlet valve of the filter device, open the liquid inlet valve, and use the first transfer pump to pump the supernatant in the product collector into the filter device, and then open the drain valve, so that the filtrate flows into the liquid separator, and stand in the liquid separator for 1h to fully stratify, and pump the separated extract solution dissolved in bio-oil into the solvent evaporation device through the second delivery pump; finally , the solvent evaporating device is used to remove the solvent from the bio-oil-dissolved extract, and the remaining product is the obtained crude bio-oil.
试验结表明：花生秸秆连续液化生成生物油产率在22％，热值在35MJ/kg左右，含氧在15％左右，油产率比间歇液化油产率(20％)稍高，品质相当。The test results show that the yield of bio-oil generated by continuous liquefaction of peanut straw is 22%, the calorific value is about 35MJ/kg, and the oxygen content is about 15%. The oil yield is slightly higher than that of intermittent liquefaction oil (20%), and the quality is equivalent .
实施例五：Embodiment five:
以猪粪为例进行液化反应试验，具体包括以下试验步骤：将猪粪与去离子水调和为1:9的比例混合均匀，并加入碎料装置以将物料粉碎为粒径小于或等于1mm的浆料后进入物料储存装置以备用；然后，通过进料管和高压柱塞泵向反应器内通入去离子水，以预热反应器，同时通过产物排出管排出预热产物，当反应器内的温度达到330℃，压力达到20MPa，开始将去离子水更换为备用的浆料，并打开物料储存装置内的搅拌装置和物料储存装置底部出料口阀门，以将浆料通入高压柱塞泵中，打开高压柱塞泵的出口阀门，以向反应器内通入浆料，同时调节流量调节阀的开度，使系统可连续稳定进出料，其中，高压柱塞泵根据浆料在反应器内预设停留时间5min设计流量，另外，反应器为全混釜式反应器。反应器排出的液化反应产物进入产物收集器中，产物收集器为两个，当其中一个产物收集器内的液化反应产物收集至产物收集器体积的一半后，切换为另一个产物收集器进行收集；在产物收集器内的液化反应产物冷却至30℃左右之后，按比例加入萃取液，同时打开搅拌结构，搅拌30min进行充分萃取后静置1h，使固相料渣充分沉积至产物收集器的底部；然后，关闭过滤装置的排渣口阀门和排液口阀门，打开进液口阀门，并用第一传送泵将有产物收集器内的上清液泵入过滤装置中，然后，打开排液口阀门，使滤液流至分液器中，并在分液器中静置1h充分分层，并通过第二传送泵将分离出的溶解有生物油的萃取液泵入溶剂蒸发装置内；最后，通过溶剂蒸发装置对溶解有生物油的萃取液进行溶剂脱出，剩下的产品即为制得的粗生物油。Taking pig manure as an example to carry out the liquefaction test, which specifically includes the following test steps: mix pig manure and deionized water at a ratio of 1:9, and add a crushing device to crush the material into particles with a particle size of less than or equal to 1mm. After the slurry enters the material storage device for standby; then, feed deionized water into the reactor through the feed pipe and high-pressure plunger pump to preheat the reactor, and at the same time discharge the preheated product through the product discharge pipe, when the reactor When the temperature inside reaches 330°C and the pressure reaches 20MPa, start to replace deionized water with spare slurry, and open the stirring device in the material storage device and the outlet valve at the bottom of the material storage device to pass the slurry into the high-pressure column In the plug pump, open the outlet valve of the high-pressure plunger pump to feed the slurry into the reactor, and at the same time adjust the opening of the flow regulating valve so that the system can continuously and stably feed and discharge the material. The preset residence time in the reactor is 5min and the design flow rate is designed. In addition, the reactor is a fully mixed tank reactor. The liquefied reaction product discharged from the reactor enters the product collector, and there are two product collectors. When the liquefied reaction product in one of the product collectors is collected to half the volume of the product collector, switch to another product collector for collection ; After the liquefaction reaction product in the product collector is cooled to about 30°C, add the extract in proportion, and at the same time turn on the stirring structure, stir for 30 minutes to fully extract and then stand still for 1 hour, so that the solid phase slag is fully deposited on the product collector bottom; then, close the slag outlet valve and the liquid outlet valve of the filter device, open the liquid inlet valve, and use the first transfer pump to pump the supernatant in the product collector into the filter device, and then open the drain valve, so that the filtrate flows into the liquid separator, and stand in the liquid separator for 1h to fully stratify, and pump the separated extract solution dissolved in bio-oil into the solvent evaporation device through the second delivery pump; finally , the solvent evaporating device is used to remove the solvent from the bio-oil-dissolved extract, and the remaining product is the obtained crude bio-oil.
试验结表明：猪粪连续液化生成生物油产率在30％，热值在33MJ/kg左右，含氧在17％左右，油产率比间歇液化油产率(32％)稍低。The test results show that the yield of bio-oil generated by continuous liquefaction of pig manure is 30%, the calorific value is about 33MJ/kg, the oxygen content is about 17%, and the oil yield is slightly lower than that of intermittent liquefaction oil (32%).
在本说明书的描述中，具体特征、结构、材料或者特点可以在任何的一个或多个实施例或示例中以合适的方式结合。In the description of this specification, specific features, structures, materials or characteristics may be combined in any one or more embodiments or examples in an appropriate manner.
以上所述，仅为本发明的具体实施方式，但本发明的保护范围并不局限于此，任何熟悉本技术领域的技术人员在本发明揭露的技术范围内，可轻易想到变化或替换，都应涵盖在本发明的保护范围之内。因此，本发明的保护范围应以所述权利要求的保护范围为准。The above is only a specific embodiment of the present invention, but the scope of protection of the present invention is not limited thereto. Anyone skilled in the art can easily think of changes or substitutions within the technical scope disclosed in the present invention. Should be covered within the protection scope of the present invention. Therefore, the protection scope of the present invention should be determined by the protection scope of the claims.
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