TW201118162A - Method and apparatus for the treatment of material and fuel - Google Patents

Abstract

The invention relates to a method and apparatuses for the production of materials or fuels, humus, Maillard or Maillard-like reaction products from a solid-fluid mixture of water and a carbon-containing component and for the treatment thereof, wherein the the solid-fluid mixture is treated at a temperature of over 100 DEG C and a pressure of over 5 bar. Feed materials are thereby fed continuously to a first reactor via a heat exchanger, and the reaction mixture is fed from one to a following reactor in a batch mode, and reaction products are continuously discharged from a last reactor.

Description

201118162 VI. Description of the Invention: [Technical Field of the Invention] The present invention relates to a method and apparatus for producing a material or fuel, a humus, a Maynard reaction or the like from a solid-liquid mixture of water and a carbon-containing compound. The Millard-like reaction product is used to treat the products, wherein the solid-liquid mixture is treated at a temperature in excess of 10 ° C and a pressure in excess of 5 bar. The feed material is fed to the first reactor in a continuous manner, and the reaction mixture is passed from one reactor to the next in batch mode, and the product of the reaction is released from the last reactor in a continuous manner. [Prior Art] In 1913, the postdoctoral thesis of Friedrich Bergius stated "the use of high pressures in chemical processes and a reproduction of the development processes 〇f For the first time in coal), in the experiment without reaction, the reaction can be obtained from wood or cellulose under the reaction conditions of Pal at a temperature of 245 ° C to nearly 340 ° C. Coal. The carbon content is usually higher in elemental analysis, while the exothermic reaction of cellulose is calculated using the Bergis method, which was used in 2006. The month has been confirmed by Potsdamer's Max-Planck_inStitute flir K〇n〇id _ Grenz, who is also known as Professor Markus Antonietti of Cancan, who has not only discovered and published the calculation of this exothermic reaction on a laboratory scale. At the same time, it was named hydrothermal carbonizatioii. In the hydrothermal carbonization method, biomass (bi〇mass) was placed in the experiment. The pressure cooker ^, and the condition of the pressure cooker is a pressure of 1 bar, a temperature of 18 〇. 〇, and convert the biomass to a material of approximately carbon (carb〇n_like) in a half time, or in the initial step The biomass is mixed with water. For the recovery of fuel products as energy, wet biomass must be consistent under long-term conditions, but due to lack of efficiency, 3 201118162 has its use. Limitation. The carbon dioxide emissions from burning fossile energy carriers are considered to be mainly responsible for climate change. In German patent DE 19723510, the biological residue treatment device consists of a cylindrical reactor in which food The waste is carried out under a temperature pressure by a temperature pressure hydrolysis process or a thermal pressure hydrolysis. The reactor is a loop reactor having a heatable casing surface (ι00ρ) Reactor. After the suspension is confirmed by the pump, a flow is generated in the reactor. The object of the invention is to develop a process by which fuel, humus, carbonaceous material and Maynard or Maynard-like reaction products can be produced economically and efficiently from a solid-liquid mixture, in particular Applicable to Industrial Regulations The purpose of the present invention may be achieved by the subject matter of the independent § 青青, and further developments may be more apparent from the accompanying claims. The process according to the invention is such that the carbon-containing solid-liquid mixture and/or the feedstock are additionally treated before and/or during the process of treatment and/or reaction, and the intermediate secondary product and/or the final product are adjusted ( C〇nditi〇ned) or processed. A facial mask that is re-enhanced in reaction or reaction and/or reaction, a solid pre-step or a pre-treatment and a solid-liquid mixture. The product of the grade and / or the final product, the material of the two carbon materials and / or the surface reaction surface of the Lions reaction yarn has increased substantially in a cost-effective manner. VIII In the process of active use of the quality, 4 degrees of carbon dioxide will be released into the atmosphere for the plant. Because ί ΐ 政 2: The use of materials has no effect on carbon dioxide, so there is no room for climate. In addition, it is produced on the effective use area of agriculture, for example, as a humus as a oxidized sultan (C〇2 藏). Without such considerations and without the active use of non-stone 201118162 chemical fuels and renewable raw materials, the climate protection and other targets set out in the Kyoto agreement will be difficult to achieve. In the method of the present invention, using biomass to produce fuel, the amount of carbon is reduced in the conversion process, and the proportion of carbon is much smaller than other methods. During the orderly conversion process, there will be a small amount of carbon or no loss of carbon. In the alcoholic fermentation (alcohdic fermentati (m) program, there is a carbon loss of 30%, conversion to biogas (bi〇gas), about 5% of carbon loss, wood carbonization treatment (W〇〇d Carb 〇niZati〇npr〇cess) about 7 〇〇 / 〇 carbon Dong loss 'and composting process (composting process) has more than 90 〇 / 0. This can be released in the form of carbon dioxide or lion ethane These gases are considered greenhouse gases and are harmful to =. The present invention is not the case of this method. In the method t of the present invention, the carbon dioxide reduction is almost no money and only the minimum weight. The method disclosed in accordance with the present invention is highly efficient. Relatively speaking, ^ bio or precipitates (4) (4) can be compared with her: : 3% to 5% can be 4 benefits have _ estimated net efficiency exposure method 'only very little or even no mine tenderness (biQgas pi (four) Compared with most methods of converting this hair into fuel, water is lacking in the process of the former. The limitation of the method of turning into energy is the lack of efficiency, the most important challenge of the energy utilization of the secret substance. i. content. However, the method disclosed in the present invention 201118162 benefits. When treating a solid-liquid mixture such as biomass, the treatment reactor which is further subjected to high temperature and high pressure can have specific characteristics. Therefore, in the reaction The inner side surface may have a surface that is anti-hybrid or, because of the extreme, a suitable coating on the inner side surface. In addition, a mixing device for the solid-liquid mixture is also provided. 13 The present invention relates to a method- For the production of materials and / or fuels, humus and / or Menard reaction products or Menard-like reaction products from carbon-containing gj • liquid mixtures, wherein the solid-liquid mixture at temperatures above 10 (rc and pressure) The treatment is carried out in excess of at least one hour and for a period of at least one hour. According to a further embodiment of the invention, the method is carried out in a semi-continuous or continuous manner, which means in particular in the reaction In the process, the treatment of the solid-liquid mixture is not carried out in a discontinuous manner (that is, in batch mode). The temperature and pressure ratio are mainly maintained within an operating range to optimize the utilization of the reaction space. And the residence time is short. The feedstock, catalyst, process water, and other intermediates of the unconverted feed may be removed or reused as needed, while the contraries, reaction products, intermediates, secondary products, and/or ultimately The product may be removed from the reaction space as the process proceeds. These and further process steps, such as the described process water, wastewater, vent gas, reaction products, intermediates, secondary products, and/or final product adjustments and/or Or scavenging to be carried out simultaneously in a continuous reactor or delayed or at intervals. For the purposes of still further embodiments of the present invention, Adjust the temperature above 160p' or between 16 (TC and 300 °c, or between 185 °C and 225 °C, and / or make the temperature can be automatically controlled. y in the present invention The purpose of further embodiments is to adjust the pressure above 7 bar, or between 1 bar and 34 bar, 10 bar and 17 bar, 17 bar and 26 bar or between 26 bar and 34 bar. The purpose of a further embodiment is that the treatment time is at least 2 hours, 3 to 60 hours, 5 to 30 hours or 3 to 60 hours 'especially 6 to 12 hours or 12 to 24 hours. In this issue 6 201118162 For purposes of still further embodiments, the processing time or conditions are selected based on the type of feedstock material, and/or the solid-liquid mixture and/or the product to be reacted. For the purposes of still further embodiments of the present invention, at least one feedstock and/or solid-liquid mixture is pretreated, the preferred way of which is by dewatering, comminution, Preincubation, mixing and/or preheating under auxiliary materials. Partial pretreatment can be carried out in an acidic or acidic medium with a pH-value of less than 6, 5, 4, 3 or less than 2. The time required for each step is reduced after increasing the degree of grinding and lowering the pH. The cultivation under the conditions of the acid pH can be carried out after the pulverization. A further progressive embodiment of the invention aims to pulverize the feed material and/or the solid-liquid mixture before, during and/or after the treatment, preferably by chopping or smashing. . The particle size of these ground solid-liquid mixtures should be less than 10 cm (cm), or less than [cm] or less than 2 mm (mm). At least one water is added before or during the treatment. The catalyst and/or aqueous solution without or without water is added to the solid-liquid mixture or at least one of the raw materials. The catalyst contains one or several different components. These ingredients are combined to form a catalyst mixture. The composition of the catalyst may be carboxylic add', especially in the preferred mode, the protic acid (tetra) her acid may be used. It is particularly advantageous to use a secondary (di-) or tertiary acid to acid (6) and all of the above grades of carboxylic acid or tartaric acid and citric acid. Citric acid and tartaric acid are crystalline and non-toxic. Both of these acids are present in fruits (lemon contains citric acid and grapes contain tartaric acid) but strontium can also use inorganic acids such as sulfuric acid such as acid. The acid can act as a component of the catalyst' simultaneously in the biomass culture step to produce an acid medium. Furthermore, more particularly, the catalyst or catalyst mixture may comprise, or in addition to, the metal and/or metal compound fine oxime C0mp0und). The above metals may be subgroups Ia, IIa, Iva, 7 201118162 of the periodic table of the chemical elements.

Transition metal of Va, Via, and Vila, such as iron, nickel, cobalt, copper, zinc, rhodium, palladium, silver Iron, vanadium, chromium, tungsten, molybdenum and/or titanium have proven to be particularly advantageous for iron or iron salts. Metal oxides of these metals may also be used, such as vanadium oxide (V2O5), copper oxide (CuO), zinc oxide, and/or chromium oxide (Ci*2〇3). . In the periodic table of the chemical elements, a metal such as alumina (Al2?3) in the main group can also be used as a catalyst in an advantageous manner. In addition, 'or instead' biocatalysts (bi〇catalysts) can also be used prior to solid-liquid mixture treatment to accelerate the conversion of solid-liquid mixtures into fuels, carbon-containing mixtures, humus and/or Maynard or Maynard-like reaction product. Thereby, for example, enzymes, micro-organisms (especially bacteria and/or fungi (ftmgi)), plant cells (vegetabie ceu), animal cells and/or cells are free or Used in a fixed form. Due to the extreme conditions in the treatment of the solid-liquid mixture, only the biocatalyst can be used in the treatment of the solid-liquid mixture, especially the pretreatment or conditioning of the reaction and/or secondary products. A further embodiment of the present invention is directed to mixing at least one feedstock material and/or mixing solid-liquid mixture prior to treatment and/or during processing. The manner of mixing is preferably a stirring, mixing , suspending, and/or agitating. Thereby, the mixing can be carried out by one or a combination of a plurality of mixing devices, in particular a combination of different mixing devices, which can be at least one jet vacuum pump, liquid jet mixer or nozzle. . According to the present invention, the mixing device preferably does not require any movable components in the reaction space when mixing. A further embodiment of the invention aims to dry the reaction after treatment with a dryer or a combination of different drying methods, the drying process comprising a convection or contact drying device 201118162 Or a fluidized and/or ribbon and/or fluidized bed drier. A further embodiment of the invention aims to remove process water accumulated in the process. The manner of removal is preferably to remove or reduct the process water to the reaction mixture by at least one solid-liquid separation device. The solid-liquid separation device may be a microfiltration device (micr〇_), an ultrafiltration device (ultra-) or a nanofiltration device (nanoflltrati〇n) and a reverse osmosis method or a combination of the above various devices. Included is a device having a ceramic filter element or having a rotating disk and/or a centrifugal membrane filter. A further embodiment of the invention aims to clean accumulated wastewater in a mechanical, chemical or biological manner. A further embodiment of the invention aims to clean or treat, in a mechanical, chemical and/or biological manner, the exhaust gases accumulated during processing, processing and/or conditioning. The present invention relates to a process, particularly a continuous or semi-continuous process for the industrial production of different reactions, intermediates, secondary products and/or final products. Reaction products, intermediates, secondary products, and final products can range from coal (Peat-) or peat (turf-) fuels to lignite (coal-like fUd), humus, Maynard or Maynard-like reaction products, such as insulating materials, nano sponges, pellets, fibers, ^able, active coal, or A carbonaceous material such as a sorption coal-based material or a charcoal-substituting material has a highly compressed carbon product and material, and particularly a feedstock for graphite and a graphite-containing or graphite-like product. Carbon fiber and composite feedstock and fiber composite material. A y A further embodiment of the invention has the object that the solid-liquid mixture contains a portion of the biomass. By using the pressure and heat supply, the 9 201118162 principle of hydrothermal carbonization allows for efficient and highly economical release according to the present invention when initially depolymerizing and hydrolyzing biomass with humidity. Exhaust heat. The polymerization of the resulting monomer causes the carbon-containing reaction product to develop within a few hours. After a short reaction time, biomass produces an increased carbon content fuel at the beginning of other processes or during further progress of the reaction, which may be suitable for energy production. According to the process of the present invention, the present invention also provides for the production of different reaction products, intermediates, secondary products, and final products, including fuel production, from coal (peat-) and lignite (lignite) to coal-like fuels (coal). -like fiiel), humic, Maynard or Maynard-like reaction products such as insulating materials, nano sponges, pellets, fibers, cables, activated carbon (active coal) or sorption coal-based materials, charcoal substitute materials, etc., carbonaceous materials having highly compressed carbon products and materials, and particularly for graphite and graphite-containing or graphite-like Feedstock feedstock for the product as well as carbon fiber and composite feedstock materials and fiber composite materials. According to the invention, the method produces energy from biomass at the initial step, wherein the fuel produced by the method according to the invention can be used for energy generation by adjusting the fuel. The adjustment state may include the production of powdered pellets or a charcoal (briqUette) or humus-like fuel. An advantage of this embodiment is that it provides a fuel that uses an adjusted state for power generation and particularly for combustion. According to the present invention, a method can be implemented which, when using the fuel produced according to the present invention, is a method of producing two forms of energy in different forms. The different forms of energy include thermal energy and/or current or a combination of two. . According to the present invention, the energy generated by different renewable energy sources has a combination of materials, including regenerative secrets, combustion stone water power, too and/or wind power, and storage and energy ages of various energy sources. The use of the steps has other _ body, liquid and milk fuels, and the fuel produced using the method according to the invention. The present invention further relates to a method for generating energy, and the method of using the steam turbine and/or gas turbine, when using a method according to the present invention, can be combined. Storage wind energy 'specially refers to pressurized air or Dispatchable Wind Power System (DWPS). The invention further relates to the use of materials or fuels produced in accordance with the present invention for the production of energy from biomass. The present invention also provides an apparatus for achieving efficient treatment of a solid-liquid mixture under industrial scale conditions. It is an object of still further embodiments of the present invention to provide a reactor constructed from a cylindrical basic body and/or under pressure-resistant conditions. It is an object of still further embodiments of the present invention to provide a reactor comprising a cone-shaped substrate wherein the angle of the tapered substrate is about 45 degrees or less relative to the axis of the reactor. 40 degrees or less than 35 degrees. A further preferred embodiment of the invention is directed to the inner space of the reactor 'particularly the bottom layer or part of the wall and the parts of the apparatus in contact with the medium, by heat exchanger (heat The exchangers and other devices and troughs are constructed of heat-resistant and corrosion-resistant and water-repellant materials, among which heat-resistant and corrosion-resistant and The water-repellant material may be a coated metal 'especially a noble metal, a pottery material or a material having an enamel. The internal space of the reactor, especially the area of the bottom layer or the wall, and the base and other components that are in contact with the reaction mixture are completely or partially surface treated and/or coated with a coating material. To prevent or reduce the caking or deposition of components of the reaction mixture. The coating material preferably comprises an anti-corrosive, wear-resistant and/or waterproof material, in particular a metal or ceramic material and alloy, in particular chromium, nickel, molybdenum, titanium, aluminum, niobium and tantalum, iron, cobalt, tungsten, Boron and carbon, and especially titanium. In particular, it is provided that the coating material is applied by a coating method, such as electroplating, which is particularly preferably referred to as a high-velocity oxyfUel, such as a high-speed oxyfUel (figjjje). HVOF). A further embodiment of the invention aims to provide a film member in the interior of the reactor. The film member has perforations, each of which has a distance of less than 10 mm ′. The preferred distance is less than 6 η, and the better distance is less than 4 rmn. If the film member is made of a sheet metal, it may be referred to as a sheet metal film because of the perforation. Some thin film components can be used in the reactor. For the purpose of a further embodiment of the invention, the perforation diameter of the film member is less than 400 um, in particular less than looum, more particularly less than 35 um. For the purpose of still further embodiments of the present invention, the holes of the film member are in the shape of a funnel. It is an object of a further embodiment of the invention to have a cavity between the walls of the perforated film member f reactor. The membrane member is attached to the inner wall of the reactor to divide the cavity into two spaced apart regions. In the embodiment disclosed in US Pat. Wire welding, whereby the weld zone defining the fluid passage can be expanded or supported by injecting a high pressure medium between the components or between the plates, thereby tempering the liquid Or the heat exchange medium can flow through the passage between the outlet and the inlet or the junction. In this publication, the double wall of the reactor can serve as a heat exchanger at the same time. The purpose of a further embodiment of the present invention is to provide a reactor inner wall designed in the form of a double wall whereby at least a cavity is formed between the inner and outer side walls. As described in U.S. Patent No. 4,700, 445, the double-walled or sheet-like plate can be attached to the cavity in a paste-like manner such that the cavity is formed into two regions. One of these areas has a population and another one with an exit or a link. The connection between the walls can be made by point or linear welding, whereby the non-welded area can be expanded or supported by the element or between the plates, thereby tempering the liquid (temperingliquid) ) or hot cross 12 201118162 The changing medium can flow through the passage between the outlet and the inlet or the junction. In this publication, the double wall of the reactor can serve as a heat exchanger at the same time. A further embodiment of the invention is directed to a reactor, a tube, a CyCie reactor, a loop (ι), and/or a stirrer. The reactor and/or preferably a thin film reactor and/or a fluidized bed reactor. At least one reactor or a combination of different reactors has at least one characteristic and a preferred combination is a spliced, tubular, cyclic reactor and preferably a loop or disturbance reactor, especially At least one membrane reactor and/or at least one circulating fluidized bed production unit. It is an object of still further embodiments of the present invention to provide a reactor having a tempering or heat exchange system coupled to at least one control unit. The blending system comprises, at least in an advantageous manner, a screwh heater, at least one heating and cooling coil, at least half of the tubular coil welded to the reactor wall, at least one heat exchanger tube Or a flat sheet and/or at least one film member or a perforated bottom layer and/or inner wall. The blending system comprises a double wall or a double tube structure of the reactor. For the purpose of a further advantageous embodiment of the invention, all of the means of the reactor through which the medium passes, including a membrane member having perforations, a jet vacuum pump or a helium liquid jet mixer, a pump, and a nozzle (n〇zzle) ) It can also be a component in a blending system. The present invention also provides a device having a non-mechanical combination, meaning that there are as many mechanical and/or movable components as possible. It is an object of still further embodiments of the present invention to provide a mixing apparatus for mixing, agitating, and agitating the contents of a reactor. Mechanical agitation and a mixing system with or without moving elements can be used to transfer kinetic energy to the contents of the reactor. It is an object of a further embodiment of the invention to provide a mixing device that does not have a movable element and that includes at least one jet vacuum pump or liquid jet mixer, at least one liquid pump and/or at least one nozzle. The object of a further embodiment of the invention is to provide a mixing device, in particular in the suction region, which is designed to be 13 201118162 to cause turbulence and shearing in this vacuum zone. A shear load breaks and breaks up the solids (de_aggi〇merate). It is an object of a further embodiment of the invention to provide a grinding device 'more particularly to grind the solids in a reactor, the grinding device comprising at least a mill and/or a chopper (ch) 〇pper). It is an object of still further embodiments of the present invention to provide a drying apparatus that includes at least one convective drier or contact drier, or flow and/or Or belt drier ° It is an object of still further embodiments of the present invention to provide for the adjustment of process water during operation. A preferred device is a process water conditioning plant comprising at least one filter (Sieve), a filter, a hydrocyclone, a centrifuge (centrifuge) or an electron/ Electrical or magnetic separation device The process of water conditioning mainly separates solids from the reaction mixture. The process water conditioning apparatus comprises at least one process water reservoir and/or at least one solid-liquid separation device. In an advantageous embodiment of the invention, the process water regulating device comprises at least one filter, a transition device, a centrifuge, a hydrocyclone unit, and a force field supported separation device or A combination of these devices. The process water conditioning device can be composed of different or identical separation devices. The program adjustment device also includes at least one filter device, in particular a rotary disk filter, preferably a ceramic rotary disk. It is an object of still further embodiments of the present invention to provide a biological waste water conditioning plant comprising at least one bioreactor, particularly a biomembrane reactor. The bioreactor further comprises at least a loop reactor. It is an object of still further embodiments of the present invention to provide a loop reactor which includes at least one nozzle for mixing a gas and a liquid. It is an object of a still further embodiment of the present invention to provide a one-circuit reverse type 201118162 having a tube and allowing fluid to flow from top to bottom. It is an object of a further embodiment of the invention to provide an air cleaning device, in particular comprising at least one air cleaning device for cleaning and/or outlet air, in particular an air filter. (ak filter). The use of a device according to the invention for producing fuel, carbonaceous materials and a utility material, a humus and/or biomass Maynard or Maynard-like reaction product may also be provided. The present invention also establishes an energy efficient generation of energy for biomass fuels on an industrial scale, where at least one configuration is provided for energy generation. It is an object of a further advantageous embodiment of the invention that the energy-generating configuration comprises a combustion apparatus that utilizes solid fuel from biomass, wherein the fuel produced by the apparatus for treating biomass according to the present invention can be directly It is burned and this fuel can be used to generate combustion gases and water vapor. The combustion, the system is coupled to the turbine and the generator such that current can be generated by the fluorine and water vapor generated in the combustion equipment. With the arrangement of the present invention, it is possible to produce in the hybrid rail-air program with the highest possible efficiency, and it is possible to achieve an efficiency of more than 43%, a better ride of 46%, and a shop. The method of preventing rot- _ phenomenon 'by purifying the high-temperature flue gas (4) fl to reduce the temperature of the equipment to the reaction 1 'the temperature of the equipment reactor to operate, which is produced according to the invention Under the miscellaneous items, the configuration of the raw materials, secondary products and/or final energy production may include a pellet furnace (four) w oven or 15 201118162 carbon ash burning power equipment, among which Circulating pressurized fluidized bed combustion combined cycle (PFBC) or combustion carbon composite cycle power technology, such as pressurized pulverized coal combustion (PPCC). The energy generated configuration can include a carbon fUel cell. It is an object of still further embodiments of the present invention to provide a device for treating biomass comprising at least one reactor for containing biomass, and at least one for treating biomass and/or adjusting reaction products and/or Or a device for secondary products. It is an object of still further embodiments of the present invention to provide a tubular reaction apparatus, a circulating reaction apparatus, and particularly advantageously a loop type reaction apparatus, a stirred reaction apparatus, and/or more preferably a thin film type reaction type. Or a fluidized bed reactor. More preferably, the reactor comprises at least one membrane component and/or means for producing a circulating fluidized bed. At the same time, the temperature of the reactor is at least l ° ° C and the pressure system is higher than 5 bar. For the purposes of still further embodiments of the present invention, several reactors for containing and processing biomass are provided to increase the capacity or flow rate of the apparatus. And these reactors can be connected in series. For the purposes of still further embodiments of the present invention, the reactor is provided with a blending system' which is coupled to at least one control unit. The blending system can include a screw-in heater, at least one heating and cooling coil (heating (6) cooling c〇il), at least half of the tubular coils are placed on the reactor wall in a welded manner, and/or at least A heat exchange tube or heat exchange plate. The blending system can also comprise a double wall reactor or a double tube (d〇ubie tube) reactor. It is an object of still further embodiments of the present invention to provide a mixing apparatus for mixing, agitating, and agitating the contents of the reactor. The reactor can be provided with mixing, agitation, agitation and/or cleaning means. In a still further embodiment of the present invention, a grinding device is provided, in particular, in which the solids are ground in a reactor, and the grinding device comprises at least one mill or at least all choppers. It is an object of still further embodiments to provide a dry pack of at least one pair of flow dryers or contact dryers, preferably flow and/or belt dryers. Natit's more advanced step-by-step embodiment is adjusted during the operation, Cheng Shui. The apparatus is a process water conditioning apparatus which may include at least one filter, a filter, a hydrocyclone, a centrifugation, and a device. The process water adjustment function mixes the solids from the reaction: the two are separated/exited. The process water conditioning apparatus includes at least one process water reservoir and/or at least 2 strike λ separation devices. In an advantageous embodiment of the invention, the process water conditioning package 3 is at least one of a filter, a filter, a centrifugal separator, a hydrocyclone, an electrical or magnetic separation device or a combination of these devices. The program adjustment device may comprise a combination of different or identical separation devices. The process water adjustment device may comprise at least one boring device, in particular, having a terrarium, or a turret filter device and/or a centrifugal membrane filter device. For the purpose of still further embodiments of the present invention, there is provided a biological, physical device or hydrophobic adjustment device or a combination of these devices, preferably comprising at least two separate devices, a biological reaction H, preferably It is a biomembrane reactor, a reverse osmosis membrane, a microfiltration (microflltrati〇n), an ultrafiltration (10), a postal (10) (four), and/or a wet oxidation. The bioreactor comprises at least one loop reactor. In an object of a further embodiment of the invention, an air cleaning device is provided, which in particular comprises at least one cleaning program and/or air placement, in particular an air filtration device. The apparatus used in the present invention is used for energy generation, especially current. The present invention provides a material and/or fuel which, in contrast to known fuel materials, has a preferred property in accordance with the methods disclosed herein. The object of the present invention is to produce a fuel or a material from biomass. The carbon fraction is higher than the biomass according to the mass fraction of the component (dry mass) compared to the biomass. % to 300%. According to the material of this case and / 17 201118162 or fuel containing peat fuel, lignite to coal-like fuel, humus, Maynard or Maynard reaction products, and carbonaceous materials such as insulation, nano sponge (nano sponge ), pellets, fibers, cables, pure, purest coal and ultra-pure coal are active coal or sorption coal materials, charcoal replacement materials (charcoal substitute material), a highly compressed carbon product and material, particularly a feedstock for graphite and graphite or near graphite products, as well as carbon fiber and composite feedstocks and fiber composite materials. Compared to biomass, based on the mass fraction (dry mass) of the component, the fuel and/or material according to the present invention comprises a carbon fraction which is increased by 10% to 300%, 50% to 300% or 100% to 300%, especially 200% to 300%. Alternatively, the fuel and/or material according to the present invention has a carbon content increase of 5% to 200%, 10% to 150% or 1%, based on the mass fraction (dry mass) of the component compared to the biomass. Up to 120%, especially from 5% to 10,000%. The fuel and/or material according to the present invention further comprises a carbon fraction of 5% to 90%, 55% to 80% or more than 98%, respectively, based on the mass fraction (dry mass) of the component compared to the feed material. . In a further embodiment of the purpose of the method, the hydrogen fraction of the fuel and/or material is reduced by 1% to 300%, 5% to 200%, and 20, respectively, based on the mass fraction (dry mass) of the component and the biomass. To 1〇〇〇/0. According to a further embodiment of the quality of the product, the fuel and/or material is reduced by 1 〇 / 〇 to 3 _, 5% to · % according to the sizing rate of the component (dry 虿) compared with the feed material. And 15 to ·/〇. The leaf (four) knife and sheep, the step-by-step example, respectively, reduce the nitrogen content of the component according to the mass fraction of the component and/or the material by 1% to 300%, especially. Up to 2j0%, particularly preferably 15% to 1%. $Quality based on the fuel and/or material according to the invention can be compared to the initial fuel value, especially biomass. 3 _ copper material because 201118162 Friendly combustion characteristics, such as low ash, lower chlorine, nitrate, sulfur, and heavy metal content, and dust or particles, fine dust and gas toxic substances including nitrogen and sulfur oxides have lower diffusion . The fuel and/or material according to the present invention further comprises a relatively high reactivity and a low combustion onset temperature as compared to biomass or petrochemical solids or biomass fuels. When the fuel and/or material according to the present invention becomes sufficiently porous, it can be crushed with a lower energy consumption than a solid fuel having a comparable fuel value or carbon content. According to the small particle size of the material and/or fuel according to the invention, it is therefore possible to have a large surface area, in particular a particle size of from about 2 um to 50 mm, a particle size of less than 1 mm ' and also less than 2 〇〇. Um. According to the fuel and material of the present invention, since the particle diameter is small and has a large surface area, drying can be easily performed. The material and/or fuel according to the invention comprises a Maynard or Maynard-like reaction product. In an embodiment of the invention, the biomass, material and fuel are produced according to a method comprising at least the following steps: treating at a temperature above 1 〇〇〇c, at a pressure of 5 bar and at a treatment time of at least one hour. Adjustment of biomass and biomass treatment and/or reaction products, intermediates, secondary products and/or final products. . The temperature can be adjusted to more than 16 〇 ° C, or it can be adjusted between 16 〇 and 3 〇〇 ° C, and can also be adjusted between 185 〇 c and 225 〇 c. The pressure can be adjusted to at least 7 bar, or between 10 bar and 34 bar, or between 10 bar and 17 bar, between 18 bar and 26 bar or between 27 bar and 34 bar. The treatment time is at least 2 hours, preferably 3 hours to 6 hours, or 5 hours to 30 hours or 31 hours to 6 hours, more particularly ό hours to 12 hours or 13 hours to 24 hours. After the biomass treatment, the reaction product is dried by means of a drying device, which may be a convection drying device or a tactile drying device and has a flow and/or belt and/or fluidized bed drying device until 6% to 25%, 10% to 20 〇/〇 or 12°/. The desired residual moisture content to 15%. 201118162 The reaction products, intermediates, secondary products and final products of the process as described above range from peat fuel, lignite to coal-like fuels, humus, Maynard or Maynard-like reaction products, and carbonaceous Materials such as, for example, insulating materials, nano sponges, pellets, flers, cables, purest coals and ultrapure coals or active coals Or sorption coal-based materials, charcoal substitute materials, 'highly compressed carbon products and materials, especially for graphite and graphite or near graphite products, and carbon fiber and composite The feed material and the fiber composite material are composed. The invention further relates to the production of materials or fuels produced by the energy production of biomass in accordance with the present invention. Biomass · Relative to fossil fuels, including renewable raw materials that can be supplied as domestic energy carriers in the long run, as well as liquid and solid organic substances and biological and biochemical process products and their conversion products, which are sufficient for this method The high carbon content, or the composition and characteristics of the fuel-containing process according to the invention, can also be treated as economically valuable reactions, intermediates, secondary products and final products. Feedstocks are, for example, in the following: carbohydrates, sugars and starches, agricultural and forestry products, especially the cultivated energy plant ( Such as fast-growing tree species, reeds, or whole grain plants, etc., soy, sugar cane and grain straw, and bio residues (bi〇genous residual) ), waste substances and secondary products, plants or plant residues from different sources (such as grass borders, landscaping cultures, etc.); agricultural waste includes straw, sugar cane (sugar cane) Leave), abandoned grain (wastegrain), 4 unsold agricultural products such as: Fan or beet (beet), decomposition of silage Hungarian parts and other feed residues, grass clipping, valley Rice, vegetable leaves, sugar cane leaves, carbon residue and waste materials with organic waste, household and factory waste high calorie fraction (residue), sludge (sludg^)', 'different types and grades of wood It includes forests (forest W〇〇d), wood 20 201118162 (timber), old sputum, saw residues and waste produced by food weiwei, including yuyu and food waste, waste vegetable, waste oil and Paper and pulp, textiles, in particular, natural fibers and natural polymers and animal wastes, including liquid feces, horse wings and poultry excrement. The body and especially the body of the animal can be counted as a biomass. In the present case, the treatment of the feedstock and/or the solid-liquid mixture can be recognized as all effects or effects on the solid-liquid mixture, which can convert the solid/kun compound into a reaction product, especially Providing energy for the initiation and maintenance of the conversion reaction, including treatment of the solid-liquid mixture at temperatures above 1 Torr (rc and pressures in excess of 5 bar. In this case, the biomass and/or solid-liquid mixture is produced. The processing of the material is to treat the feedstock, reaction products and/or intermediates in different steps before and after the chemical conversion step. The processing includes all the steps, procedures and effects or effects on the reaction participants. Including pretreatment and/or treatment. For pretreatment, all effects or effects are understood to be influential for the end of the filling process from the start of the conversion reaction until the reaction space is completed and to start the energy supply. In particular, in the reaction space or outside the reaction space, the preheating of the feedstock and the main components of the reaction mixture (ie more than 2/3 of the reaction mixture) The composition of the compound is ground to a particle size of 10 mm or less as a pretreatment. In this case, the solid-liquid mixture is a suspension, dispersion and other dispersion system. In particular, biomass. It has been found in the process according to the invention, in particular for these solid-liquid mixtures, that the liquid phase content is increased or solvent and/or solid when the reaction system is carried out physically or chemically. _Physical study response side of the _ liquid separation or there is = the amount of solid part of the rate of lasing. In this specification, the material or & s liquid or liquid-free solid system as a solid-liquid mixture Manufacture. Re-adjustment of the reaction product and/or secondary product of the present invention and 21 201118162, the entire crepe says that it includes a transformational reversion: she tends to/or all effects of the final product and _ 'store by these methods The desired or the form of the invention. For the semi-continuous or continuous method of the present invention, it should be understood that the reaction product of the experimental station and/or the worker Wei mold, the towel, the Wei product and the most 炊 ΐ ΐ 其中 are at least satisfied. As follows a rule or two or 1 姨ίί at the end. Less - face force ^, reverse wire or Lai composition internal temperature holding,, only 鬲 40 C to 90 C after at least two reaction cycles, Better temperature production from 60C to 70C and / or higher than the boiling temperature of the process water at an absolute pressure of at least 丨, direct contact with the reaction mixture for more than - minutes, so that the extended skin is directly Fine (for example, placing the handle on the wall of the reaction vessel with the H vessel wall more than the container wall) for more than - minutes without increasing the visible redness of the skin, only the device for shutting down the device and the insulator is possible.  Especially at least - the strength of the nanometer, the reaction is the composition of the device, the pressure is continuously at 1 bar absolute or the ambient pressure is passed through at least two reaction cycles. At least two containers, at least one of the reactors, are connected in a manner that can be transported, pressure equalized, or stored in a compressed medium. 3.  The processing of the feedstock, solid-liquid mixture, reaction product, secondary product, intermediate product, and/or final product or other reaction participants is carried out in a plurality or in more than one vessel or vessel in one apparatus. 〆 4.  The containers or vessels to be processed are all necessary or essential components of the apparatus and have an overall volume of at least 500 liters. Thus at least one of the containers cannot be moved by humans only, but can only be moved by means of additional auxiliary means. 5. In a reaction cycle, a pretreated carbon-containing solid-liquid mixture and/or different kinds of feed materials, biomass or carbon-containing compounds, especially different combinations and different concentrations are used. Eight 6. Solid-liquid mixtures, reaction products, secondary products, intermediates and/or final products and/or other reaction partners of different feed materials, including catalysts and/or 22 201118162 or = blending media, such as water (special * process) Water) and / or gas (Agent / σ filament) fine, time lag (time_laPsed), continuous, L = or 疋 interval supply to the reaction mixture or remove the H-like f sequence from the reaction mixture in the pressure capacity 11, Reaction 1 or * other equipment consists of t 2 i > lGCJL 7GC or higher than the full point of the process water at 1 bar absolute pressure > or t at least - absolute pressure. ^1, a coherent procedural towel', especially in a single slap towel treatment reaction mixture. Before the fine cycle or during the reaction period, the kinetic energy is introduced into the feed material or the reaction mixture to make it run. It is at least a lion or a hybrid system of any type or a combination of a lion or a mixed system. It refers to at least one non-mechanical agitation or mixing system whereby electrical operation can still be performed when a single system is used, which does not require a magnetically-secure shaft. 9.  Before the reaction cycle or during the reaction cycle, in particular using at least one system or a combination of different systems or devices, the thermal energy is introduced into the raw material or the thermal energy is dissipated by the patch, whereby if it is a single-new It should not be - as usual - _ (_) and / or shed - some hand (han separated, separated from the non-blocking junction heat transfer device and driven by electricity.  The continuous method according to the present invention is characterized by requesting items i, 36, 50, 72, 98, 103, 113, 115, 122 and 143 and these independent items j. In addition, 'for a continuous manner, the two-step rule can be obtained from the characteristics contained therein, wherein the carbon-containing feed material is fed into the first reaction-through|| in a continuous manner via a heat exchanger, and The batch is transferred to the subsequent reactor and the reaction product is released from the last reactor in a continuous manner. It can be obtained in a continuous manner, and the above-mentioned claims protect the features obtained by combining the devices and components. 3 In a container, it can be understood that there is a cavity on the inside and the top can be opened or closed. It is used in particular to separate the contents from their environment. a vessel for the conversion reaction (conversion reaction, ie treatment of the solid-liquid mixture and/or addition of the solid-liquid mixture 23 201118162 'which is a reactor closed to the outside), such as a pressure vessel or reactor space or a pressure vessel The space is formed. The vessel in which the decisive reaction step is carried out is specifically described as a reactor. The decision-making step is to be understood in particular to mean, for example, a step of operating to a greater extent in the temperature and pressure ranges, which must have an average conversion of at least 1% to 3% of the feed material to become a reaction, inter-race product as described above. One of the secondary products or the final product. _ By the existing spatial region and in a reaction or pressure vessel space to define the reaction m or the pressure capacity, the reaction conditions of the towel can be measured to be biased. The reaction conditions of the deviation occur via a structural, mechanical and fluid, and/or phase, chemical, electronic, electrochemical or other type of influence. The device for this purpose is not only for the pressure cooker for laboratory purposes, it is equipped with a power operated agitation device or a hybrid system device with a magnetically coupled single shaft, and the compression load of the external reactor wall is smooth inside. The wall side heat exchange is by means of an electrically heated outer casing which can be isolated by some grips. The reaction cycle, the period of the reaction, can be understood as the duration of a single conversion reaction, which begins by introducing the starting product into the reaction space and supplying energy to initiate the conversion reaction. One cycle begins with the reaction process until there is a desired reaction product in the reaction mixture, without post-treatment or adjustment' or until the reaction process is completed. a device that is fluidically, thermodynamically or thermally transferred to a mixture mechanically or by ultrasound, thereby causing the contents of the reactor to move by agitation or agitation, as agitation or Hybrid system. Stirring or agitation results in movement of the contents of the reactor. Moving the reaction mixture or along a pressure gradient via a device such as a pump, a liquid vapor mixture or a jet vacuum pump, a spray valve or a jet nuzzle, and a mechanical and thermal mixing device The lead reaction mixture is also part of these systems. The apparatus for carrying out the method of the invention consists of at least two devices or elements. At least two containers or vessels, at least one of the reactors 24 201118162, etc., „compressed medium connected. The condition of the equipment is not; 疋本=2; (2) J container 'in this component fails two π eight ― Will be limited, especially considering at least ten health points _ cost-effective. 7 devices or components for general use, the use of coherence 2 <^ent pn)cess). Line with dry matter =: is empty 芩 以 以 通 μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ μ Including pressure = > dish degree 'where the conversion reaction of the hydrothermal carbonization method can be carried out in excess of at least one. The end of the reaction procedure is characterized by: in the emptying of the ginseng, the system maintains at least one of the targets in the reaction program = the reaction record of the needle, and (4) the thief is the genus, the body, the liquid, and the (10) substance. The system is at or already in operation at 5 bar and the temperature is above 100. Oh, it has nothing to do with the length of the reaction space. Liquid Mixing Secrets Yi County Liquid, Residual and Other Knife = System, which includes solids containing liquids, especially biomass. According to the present invention, in particular, a paste-liquid mixture is used, in the case of a reverse-filament type, which increases the content of the solvent, and/or causes the dissolution of the paper/language/physical or chemical properties, which improves the solid-liquid. The isolate or rate of change has a higher solids content. The suspensions and dispersions are all heterogeneous solid-liquid mixtures: heterogeneous (or immiscible) substances mixed with liquids and objects: systems are understood to be suspensions. The suspension has at least one solid phase and at least one liquid phase. Colloidal dispersions, micelles, vesicies, milk 25 201118162 emulsions, gels and aerosols, for example, latex or foam, are dispersion systems 'Also is a binary mixture of small particles and a continuous dispersion medium. The Maynard-like reaction product is understood in the present context to be a compound which is an intermediate, secondary product, final product and reaction partner of the Maynard reaction product, and which may have similar chemical, physical or biological properties. Advanced glyCati〇n end products (AGE) produced by rearranging the main Amadori product, also belonging to these compounds, and further reacting to Mena The final product of the German reaction. The high glycosylation end product can form a crosslink with other proteins via rearrangement and polymerization. Due to the developmental path, highly glycosylation end products have many different and complex forms, whereby the form that has been detected so far has Νε-rebellion methyl amino acid (>^(carb〇xymethyl)lysine ( CML)), ftirosine and pentosidine. A polytetrafluoroethylene (PTFE) material is understood to be a similar, related or unrelated species of matter and compounds having at least one or some properties of polytetrafluoroethylene, such as: reaction inertness, very low friction Coefficient, very low drawency, thermal resistance, low adhesion durability of surface contaminants or flat surfaces. Fuel is a substance used for energy production and converted into energy by chemical, electrical or other methods. The material or 疋 practical material is a substance that is processed, processed, or otherwise processed or processed into a product, or a work object of the final product. The purpose of this case is illustrated in more detail below. The process of converting the feedstock or biomass material according to the method of the present invention can be roughly divided into the following stages: 1. Heating stage (heating Phas noisy biomass is in a temperature and pressure down polymerization stage (dep〇 Lymerjzati〇n) is based on the supply of steel from the source. The system refers to biomass with a high carbohydrate content, which initially has an expansion during the heating phase. 26 201118162 Swelling reaction. Containing between p〇lysaccharides in the cell wall. In the expansion procedure, gelatinous (gelatinous in a further process) structure is also temporarily formed, which will be depolymerized. Decomposition in a further process in the action phase. 2. Depolymerization phase: where the original structural protein decomposes, in particular a plant or lignocellulose biomass, which is mainly composed of a polymeric structure. Composition of polymerized structural protein cellulose, hemicellulose, and lignin. Monomers and oligomers (oligomere) in the form of carbon compounds. The higher the ratio of resistant and crosslinked structural proteins' and the smaller the surface of the feedstock, the more time is required to depolymerize. At the same time, the hydrolysis results are referred to in chemical compounds. The chemical reaction destroyed by the reaction of water. The higher the ratio of carbon compounds, non-plants and unstructured proteins and fats, the lower the proportion of lignin-cellulosic biomass, the faster this stage is carried out. At the end point, the release of heat energy increases and forms a substance similar to the feedstock oil. 3. Restructuring phase: The cyclized and non-crosslinked carbon compounds are restructured and crosslinked. Similar to the initial rough structure of the feedstock, but losing cohesion with the superstructure and thus losing its resistance and robustness. The newly formed structure with higher brittleness and porosity consists of It has a small particle diameter of several hundred micrometers to 5 nanometers and a smaller particle size in the middle and final state. The new carbon compound is similar in form to natural coal. Containing different carbon compounds and olefin derivatives, the percentage of mass of carbon and the elemental (dry mass) associated with hydrogen and oxygen fraction is reduced. Compared with fossil fuels, one of them is easier to distinguish. Characterized by the presence of a Maynard reaction product in the liquid and solid phases of the reaction product. 27 201118162 4. Stabilization phase: although the depolarization and polymerization phases are carried out exothermically, At this stage, the heat release is greatly reduced' and the reaction is completed in the stabilization phase and finally the reaction is stopped. Characteristics of the reaction product such as: degree of purity, form, structure, density, mechanical resistance or mechanical strength, particle size, surface structure, composition, combustion ( The combustion characteristics, the fUel value and the energy content depend on the method or reaction conditions, that is, on the parameters used to control the method according to the present invention (ie, the processing program). The reaction process or processing procedure is particularly affected by the following treatments or reaction conditions or standards: 1. The composition and characteristics of the precipitate or feedstock include: density, particle size, water content, purity, carbon content, inorganic content And including the test. 2. The relationship between the solid phase and the liquid phase is the relationship between the dry mass and the borrowed water. 3. Temperature, pressure and variation limits for these parameters. 4. Catalysts: selection, composition, concentration, particle size, mixing ratio, and supply time. The reaction can be accelerated, manipulated or directed by providing a catalyst or a mixture of catalysts later in the reaction. Thereby, the characteristics of the reaction product can be affected. A particle size metal catalyst is an essential part for the formation and structure of the reaction product. The considerable degree of reaction time is determined by the strength of the acid (pK value). ‘ 5. Heat exchange or blending system and temperature adjustment time, pH, concentration ratio, and these properties in process water. 6. The substance or chemical change in the reaction mixture is caused, for example, by hydrolysis: in particular, density and porosity are increased during the conversion reaction. 7. During the polymerization period, the faster the polymerization proceeds, the more pure the reaction product. 8. Methods and means of mixing or agitating the contents of the reactor and transferring energy thereto, as well as flow rate, shear stress, and mixing interval and time. 28 201118162 9. Process water: salt concentration, acid, such as chlorine (ehl〇rine), sulfur (4) (10) elements and their salts and metals and including dish & 〇Sph〇r〇us) and gasification ( Nitrate) An inorganic substance of a compound. The cleaning method of the process water during the operation and outside the operation process. 10. Concentration of contaminants, such as sand, may cause obstruction, idling, delayed reaction, or substances that cause unwanted secondary products or precipitation. 11. The type of implementation includes the strength and duration of the method steps described herein. 12. Selection, combination, synergy and control of blending and mixing systems. 13. Selection, composition, efficacy and efficiency of process water adjustment, and guidance on the need to make adjustments to the variable reaction volume through the supply or recovery of process water and materials. ^ Further method steps can be as follows: 1. Supply of feedstock, including biomass, feedstock, catalyst and water. 2. Pretreatment. 3. The feedstock is transferred to a transfer system and/or container. 4. Apply to individual processing or processing steps to transfer the feedstock to the vessel. 5. Water removal and/or drying of the feedstock. 6. The feedstock may also have a crushing of the catalyst. 7. Removal of metals and impurities. 8. Culturing using a catalyst, particularly an acid. 9. Addition of one or several additional catalysts. 10. Preheating of biomass. jL is, for example, a compaction when introduced into the reactor. 2. Introduce the pressure vessel or reaction space. 13. Heating. 14. Process water adjustment and air cleaning. 29 201118162 15. The reaction product is removed from the reaction space. 16. The reaction product, product and/or final product is separated from the reaction mixture. m 17. Drying of the desired reaction product. 18. Grinding of the desired reaction product.丄 9. Cooling of the desired reaction product. 20. Adjustments. 21. Recycling of plutonium, especially via thermal cycling or heat exchange. Prior to and after the chemical conversion process, the feed and reaction products, the inter-cloth product, the secondary filaments, and/or the final product are processed in a crucible. These processing steps are either a rainbow or a technical level (four) conversion. Therefore, = should be understood as the artificial decomposition of the knife or the processing of the bio-f and/or the reorganization of the reactants and/or secondary products. , can be married to the electronic lion or age, its characteristic coupling shaft 'and has the characteristics of the outer wall of the reactor to withstand the compression of light' inside the electric heated casing (electrically heated casing c = a ^ ier) Wall-side heat conduction is performed by some hand grips. For semi-continuous or continuous processes, the agitation or mixing system and/or the standard of the blending system described in points 9 and 10 above. It is usually possible to grind before storage of the biomass, and in particular before the actual conversion procedure, it is more specifically to grind before or after the addition of the biomass. In the case of grinding devices, it is often difficult to grind with, for example, a milling:wet grinder. Depending on the feedstock and the desired particle size, different types of fine cut, grind or wet grind are used. Particle size should be performed. Therefore, the smaller the size of the spine, the bigger the screaming. The larger the surface area of J should be, the faster the chemical conversion. The particles of the shredded organism may be less than 1 cm, or less than 1 cm, or 2 m. The energy, time and raw material results in the grinding process are determined by the process f program, in particular, depending on the form, particle size and retention length of the feed material. 30 201118162 f pH is healthy at 6, commission 5, can also be less than 4, _ is less than 2 can be less than 2, Wei Wei or miscellaneous media towel, the culture system is the time required for the pre-H 1 minute i step As the ground P is less acidic. For example, after grinding, in the positive value, the system is equipped with a double wall or another (four) system of insulation. The use of this blend is mainly due to the heat from the program according to the procedure for generating the program or its sequence, or the use of partial purification and heating. Training for at least 1 () minutes to 6 () minutes,! Small day|to 10 hours or 10 hours to 6 (H, hour. Depending on the feed material and other pretreatment steps) Pre-culture can reduce the equivalent reaction time. Under ideal conditions, save more than 3~1 〇%, 10~20% or more. Since water is chemically generated during the reaction, and the water leaving the feedstock knives is increased as the program proceeds. For example, in the subsequent The reaction capacity required for the reaction space in the reaction vessel will decrease with the recovery of water. Therefore, during the reaction, the volume of each individual reactor is reduced in terms of the cascade of reactors. Process water is obtained after the end of the conversion reaction or during the conversion reaction. During the reaction, the recovery of the process water occurs at a temperature higher than 18 〇〇c and the pressure exceeds 5 bar. This is a method for solid-liquid separation. And the device is a specific requirement. In the recent method, 'screening program (c〇arse sieving, fine sieving), filtration program and / or by cyclone (four) coffee Batch), dynamic (dyn Amic), electrostatic, vacuum, pressure and sterilizing filter-to-force/hybrid programs, especially cross-flow filtration (cr〇ss n〇w which includes microfiltration, ultrafiltration, nanofiltration and The reverse osmosis method is particularly preferred. More preferably, it is based on a hydrocyclone supported by a force field, a centrifugal method, a separation device, and a functional principle, and/or a device using a filtration method. In particular, the filtration method can be applied to the user by the reaction conditions of the hydrothermal carbonization method. The rotary disk filtration device or the centrifugal membrane filtration device is preferably used for solid-liquid separation. Different solid-liquid separation methods can be combined with each other. One reaction 31 201118162 Each reaction E after the reactor can be connected with the g]-liquid separation device. The liquid separation is performed in the form of a continuous or p-tear method, and the operation time is stopped in the reactor. At least two tenths of U can be adjusted according to the required handle and the 3 performances used. Back to the process water system sister - in the isolation of the anti-grain or pressure vessel. For the process water enrichment (enriehing), towel Process water that can be processed from s to unprocessed The storage shot is directly removed. The aspect is described in the specification of the invention of the forest - the tilting is a plurality of inspection and separation devices to make the process water_, and on the other hand, for example, in the evaporator (evap〇mt〇r) Evaporating water (^vaporating water) to concentrate the process water. The steam evaporating process generated by the evaporation process is in other positions of the program, for example, heating the feed material before entering the heat exchange, and charging the feed through the heat exchange Heating or running the reaction product, such as an airagitator mill or other drying device described elsewhere in this specification. To concentrate the process water, remove at least 1% to 5%. 5%^20% or 2()%~70°/H $ &目# 'Other methods described in this specification sheet can also be used 'eg reverse osmosis, however, the disadvantage is due to temperature sensitive film The relationship must be reduced by more temperature. The process water system is stored in an isolated and corrosion resistant vessel or, if possible, a process water storage tank that is designed to exclude air pressure vessels. The concentrated process water system is used for pre-carrying, preheating, and pumpable solid-liquid mixture production of the feedstock for the absorption in the reaction mixture for use in the reactor of the plant. The coating or addition of the feedstock, and returning to the running process, is used as a heat carrier medium (and/or as a fertilizer component) in the equipment or in further processing outside the equipment. For each use, 'process water can be obtained at temperatures above 丨 to 5 〇.

The pre-culture, preheating, pumpable solid-liquid mixture production or enthalpy of the feed material is applied or mixed for the feed material supplied in the reactor of the apparatus, preferably at a use temperature of 25 ° C to 50 ° C, 50 ° C to 70 ° C or i 〇 ° C 32 201118162 process water. For these purposes, its ^ ί 妓 4 4 is lower than 2. Warming Urt—steps in the equipment or outside the equipment, preferably using heat = however, for these feeds, the temperature exceeds the supply of the booter in the boot to evaporate or use another way to exclude a certain amount Water, itr, f acid as a transport agent to obtain the required pH value, the boiling water level of the ship is such that the point is higher than 2?9〇C ° ^^^Phoric acid) Hemp: / dish: 糸213 C. Although the boiling point is high, even if it is difficult to avoid the 5 points of the catalytic point from being dissipated by the process water, it can still be effective by lowering the boiling point of the acid such as sulfur (bivalent) stress point or decomposition temperature =; GGC 'chlorine The temperature of the Buddha's point of the iron (trivalent) is higher than 12G 〇c (sublimation), and the temperature of the axis of the bismuth iron (divalent) is Na. . The concentration of self-made water can reduce one or several catalyst components. The m steam is used in other locations in the process, such as heating the feed material before entering the heat exchanger, heating the heat oil via the heat exchanger program or using A device for drying the reaction product, such as an air agitator mill and/or a drying device as previously described in this specification. Process water vapor cleaning according to the application. In the present case, it is described that a plurality of pumps can carry concentrated process water at a temperature higher than 250 ° C. The pump can be a helical displacement pump. The temperature is lowered by the heat exchanger at ambient pressure, or the temperature is lowered before the feed is fed to the pressureless device & resupless device or sent to the mixing device, so that the temperature of the solid-liquid mixture is 50. °C ~ 60. (: or 60. (: ~80〇C. Especially the separation of metal, inorganic or sand from the biomass 33 201118162 and other impurities. These methods and procedures are used, for example, in biogas plants The treatment range of biomass and organic waste is established in the (biogas plant). After the pre-culture, the catalyst containing the added or non-added water and/or the aqueous solution may be added to the acidic medium. The catalyst may comprise at least one or several different components which together form a catalyst mixture. The composition of the catalyst may, for example, comprise an acid. The reaction procedure is to a considerable extent dependent on the choice of catalyst, composition, concentration, particle size. , mixing ratio, and time impact of supply. Therefore, these factors depending on the catalyst have a great influence on the formation, design and properties of the final product. For the final form and structure or reaction product, the particle size of the metal catalyst is formed. Part, and the reaction time is also determined by the strength (value) of the acid, for example, when the particle size is small. At ten micrometers, especially from 200 nanometers to 1 nanometer, and particularly preferably from 10 nanometers to 199 nanometers, the probability of forming a final product to homogenize the fibrous nanostructure of the morphology is increased. The smaller the smaller, the more precise and uniform the fibrous structure of the new carbon compound can be defined. However, for the production of defined nanostructures, the degree of uniformity of carbohydrate content, particle size and particle size is a trend for the reaction. Both of them play a role. The catalyst and catalyst mixture supply time can accelerate the reaction or guide the reaction. According to the desired final product, it is also useful to introduce the catalyst at a later time in the reaction procedure. The inorganic acid can also be used as an acid. In particular, mineral acids, particularly preferred are strong acids, and they have as low a PK value as possible. The reactants of these acids and acids used are non-toxic and minimally corrosive. The reactants are not detected, and the acid and the components of these acids are purified or treated as easily as possible. The sulfuric acid of the agent satisfies most of the requirements and is therefore particularly suitable. Different acids can also be combined. The carboxylic acid (carb〇xylic aCld, S)e', especially protonic acid, can be used as an option or It is particularly advantageous to use binary-decanoic acid or tricarboxylic acid and all of the above carboxylic acids, tartaric acid and citric acid. Citric acid is crystalline and free of impurities. These two types of fruit are produced naturally (the citrus fruits such as lemons contain citric acid, and the acid used as the catalyzing component can also be used to generate the acidic medium for the culture step. The concentration of the acid is especially related to the ρκ value, and About 0. The percentage of capacity of 1 to 3, the percentage of capacity of 〇 6 to 2, particularly preferably 0. A percentage of capacity from 3 to 1. The feed material is pre-cultured with an acid and can be used with less reaction time. The longer the pre-culture time, the stronger the acidity and the higher the acid concentration, and the shorter the reaction time. The catalyst or catalyst may contain one or more metals in addition to other components. It is preferred to use a transLn metal such as iron, nickel, cobalt, copper, chromium, crane, molybdenum, or titanium, and it has been found that iron has proven to be particularly advantageous. The catalyst may be added prior to introduction into the reactor, or a catalyst may be added during other times of the process. Further, the different catalyst mixtures or compositions can be added to the reaction mixture at different times. The biomass is thoroughly mixed with the catalyst or catalyst mixture. The catalyst then forms a reaction mixture with the biomass. The mixing sequence can be selectively carried out in the reactor. The compression of the reaction mixture can be carried out in one or several steps, either in the reactor or outside the reactor. High compression is advantageous, and in particular refers to the preferred use of the reaction space. The amount of compression is determined by the desired = reactant and the transferability of the reaction procedure to the reactor. For example, the reaction mixture can also be introduced into the reactor after pretreatment. For example, a preheating step can occur before the reaction is introduced into the pressure vessel space. All reactants can be preheated. Among these feedstocks, especially biomass, can be heated to near 60. (: to 90 ° C. For example, by supplying heat energy, the preheating step, especially the addition of a process water having a temperature close to the boiling point, a two preheated biomass suspension, and other water at a pressure of absolute pressure Or by supplying process water vapor or other heat source carrier. The heat energy generated by the heat exchange process can also be selectively or additionally used in this step. The reaction time is related to the desired reaction product, Between 1 hour and 60 hours, especially between 3 hours and 40 hours, more particularly 35 201118162 between 5 hours and 18 hours. When there is no more obvious en (enthyalpy;) release The reaction time can be regarded as the end 'or the reaction is considered to be terminated. The minimum pretreatment and / or omission of the individual pretreatment steps will increase the reaction time to more than 60 hours. The reaction time is related to the respective feed materials. And the composition is especially relevant. The larger the surface area, the smaller the particle size, the smaller the proportion of lignin or cellulose, and the larger the carbohydrate ratio, the heat in the depolymerization stage. The faster the release, the faster the stabilization phase is achieved, and the reaction time or residence time is reduced. The shorter the conversion time of the individual feed materials, the longer the delay in the reaction that has been introduced into the reactor, for example. A large proportion of fat or non-plant and non-crosslinking, such as animal protein or bacterial protein, can also shorten the reaction time. The termination of thermal energy release in the reaction program is an indicator of the end of the conversion process. According to the case, the temperature can be as high as 300. (:. But the temperature is between 185. (: to 205 ° C is also advantageous, especially at 215 ° C, and more particularly preferably at 225 ° C. According to the present case 'in the absence of air The pressure is between 7 and 90 bar. It is preferred that the pressure is between 11 and 18 bar, or between 18 and 26 bar, or between 26 and 34 bar. [Embodiment] The apparatus of the present invention comprises a reactor which can be developed in different ways depending on the progress of the procedure in the reactor, the type and amount of solids used, and/or the desired reaction product. According to the case At least one of the reactors may be a cascade reactor, a tubular reactor, a circuit reactor, a loop reactor (i〇〇p react〇r), a membrane reactor , a fluidized bed and/or an agitated vessel or an agitated vessel reactor, or a reactor having separate characteristics, or a fluidized bed having a different characteristics of the reactor, the plated 1 reactor is preferably Circulating. According to one of the reactors or a combination of different reactors, it can be used in the equipment for different processing time and processing steps. In addition, the reactor can be designed to press 36 201118162 according to the required pressure. The pressure vessel format is designed according to the processing procedure and the mixing technique used. In a further embodiment of the purpose of the invention, the reactor is of the type formed as a multi-membrane fluidized bed reactor having a circulating fluidized bed. This reactor combines the advantages of various thin film reactors and fluidized bed reactors. As used herein, a fluidized bed is understood to mean ballasting or aggregates of solid particles that are brought into a fluidized state by upward fluid flow. In this context, the so-called "fluidized" causes the (previous) ballast to have fluid-like properties (e.g., water properties) at this time. According to the case, the solid: liquid mixture appears in the reactor. If the solid fine particles or the particulate ballast are passed from bottom to top by a gas or a liquid (so-called liquid medium), they are agitated. The fluid medium needs to pass at a sufficiently high rate to lift the particles to agitate them. The energy input required depends on the reaction conditions. When the reaction is complete, the solid phase particles can be easily removed from the reaction space in a partial but continuous manner due to agitation. Fresh solid raw materials can be refilled accordingly. The flow rate of the fluid is adjusted so that the manner in which the solids are agitated is at least a static fluidized bed. The fluid flow rate in this state is lower than the sedimentation velocity of the particles. By combining individual adjacent particles, the fluid resistance is higher than the fluid resistance of a single particle. It is thus possible to form a suspension layer having a defined surface. The flow rate of the fluid can be increased as high pressure is applied to the membrane element. Quite a few particles are released from the basezone by higher fluid flow, while the upper boundary collapses. A certain proportion of solids will still fall back into the basement zone in the fluidized bed. A flow is formed in a so-called free space above the dense area where the solids are lifted into a thin suspension in a relatively wide core, and the solids fall off at high speed clusters at the edges of the reactor. By positioning at least four liquid stream mixers (the distribution of which is as uniform as possible in diameter and at the same vertical distance as possible), as well as additional mixing devices (which include the base metal sheet ( The surface on the base metal sheet) 'suppresses the shape of the agglomerate and the layer boundary, so that the homogenization of the particles can be carried out. + When properly used, especially when using film components, the following benefits can be achieved by the reactor according to the invention, wherein:  By accelerating the propellant and the turbulence created by the fluid flow, a high relative velocity is produced between the continuous fluid and the dispersed solid phase. 2.  Frequent particle-particle impact and particle-wall impact. 3.  Enhanced mixing of the granules. 4.  The heat exchange of the reaction mixture with the fluid is accelerated. 5.  Minimize deposition. 6.  The dosage of, for example, water and reactants is controlled during the reaction. The reactor according to the present invention may have one or more of the following characteristics. The reactor may comprise at least one pressure vessel and at least one means for solid-liquid separation, and is also referred to as a membrane reactor. The reactor may have at least one coarse screen and/or fine screen filter unit or a combination of both units, which may also be combined into one filter unit. At least one of the pressure vessels may have an agitation and/or mixing system, which may also be referred to as a stirring vessel reactor. The volume of the total reaction space of the pressure vessel or reactor may be zero. From 5 m3 to 1 〇, the cubic meter can also be from 5 m3 to 2,000 m3 and or from 5 m3 to 5 m3. The volume of the reaction space, hopper and storage space of all the vessels of the equipment containing the pressure vessel or reactor may range from 立方5 m ^ 3 to 10,000 m ^ 3 or 1 〇〇〇〇 m ^ 3 to 7 〇〇〇〇 m ^ 3 and can also be 50,0 〇 0 m ^ 3 to 500,000 m ^ 3 . Depending on the feedstock and biomass, the biomass can have a water content of up to 95 〇/〇 or more based on the total weight. For this reason, it is useful to complete the water removal process before the conversion process. Due to the high moisture content and low packed weight of many biomasses, the transportability is limited so that the initial solids ratio in the reaction space can be close to between 5% and 30%. The yield of the reaction product will be around a single percentage number relative to the total reaction space volume. Therefore, a larger reaction space 38 201118162, the system is necessary. It can be transferred to a large reaction space volume by several pressure vessels or reactors connected together. By connecting these reactors, methods such as splicing, and/or combinations of different reactor types, improved retention time distribution and higher operating capacity can be achieved by improved control of the processing program. At the same time, it can meet the different needs of the reaction phase and some of the steps. A more suitable heat exchange is carried out in a tubular reaction H-belt, with better mixing and remixing in a lion-type H or _ reactor. By singulating the entire volume of the reactor into a plurality of pressure vessels, the transfer capability of individual equipment having pressure vessels can be improved. By connecting several pressure vessels or reactors, a continuous, or semi-continuous procedure can be facilitated. At least the pressure vessel contained in the reaction n or the compression process gas contained in the reactor can be used and integrated into the equipment. Before the program gas is discharged into the atmosphere or sent to the outside or inside of the facility, it can be cleaned in the air cleaning unit (air cleaning equipment). Procedure, body, human and wet oxygen recording sequence-like oxidation procedure towel, which operates with compression null =. If the retraction is connected with the female sequence, the oxidizable component of the process gas in the process gas can be converted into heat energy and Recycling via a heat exchange program. By continuously separating or retrieving a single reactant during the processing procedure, an example can be performed in the method to increase the solid portion. The content of the body can be determined by the reaction procedure or the condition The original 15% increase to 20% or π t, f is increased to 31% ~ 45%, and more specifically 岐 46% to 70. / = = when the size of the mother reactor can be reduced while the reaction develops At the same time, the raw material of the feed can be used in a given reactor volume. The several reactors are connected in series, and the beans 2 are separated by ^valve, which further makes it possible to increase The output of the product, the storage of the material and the material Or add fresh feed material, catalyst anti f or piece goods. The reaction mixture is transferred from the pressure vessel to the next pressure. 续 Κΐΐ ί ί 续 _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ Reactor and Recording System Reduction 39 201118162 ‘The preferred material is stainless steel. The wall ΐΐΐΓ of the reactor is considered to be between 7 and 20 bar, preferably between 20 J and the bar, more particularly between 30 and 40 bar; the temperature is ^ 160 c ^ 230 c, especially 26 (rc and more particularly 3 〇 (rc. at least one pressure vessel, reactor or equipment component in the temperature sense, > _ reaction cycle system is consistently higher than Thief to Qing, special 疋 from 60 C to 7 〇 C and / or higher than the boiling temperature of the process water under the absolute pressure of 丨 ' 'This makes prolonged direct skin contact, for example, by hand directly contacting the container wall and the reaction mixture exceeds More than _ minutes without increasing the redness of the skin, only by auxiliary devices, spacers or additional devices. > The reactor according to the present invention may comprise a vertical cylindrical body. Diameter-height The ratio (cUameter-heightratio) is at least 1:0. 5, 1:2, 1:5 or greater. The upper base is an approximately spherical base. In the upper part, especially the upper half ep and especially the 2/3 part of the upper layer, it has a conical shape whose diameter gradually increases toward the bottom layer. The angle of the conical shaped base is 45 degrees with respect to the reactor axis, the lion is less than 4G degrees, and the lion is less than % degrees. The transition from, for example, the reactor wall to the substrate zone is circular to reduce disruption of the fluid. For the supply of the reaction mixture, the arrangement of the nozzles is variable, which may for example be arranged in the upper half of the pressure vessel, preferably in the upper third. The supply is via a valve through an output nozzle approximately at the center of the substrate or conical substrate. The components of the reactor and the nozzles can be joined together by welding. In addition, a cover can be installed. By preferentially utilizing a liquid stream mixer or a jet vacuum pump and a full jet nozzle (fUll jet nozzles), the diameter to height ratio can be close to 1:2 to 1:3 ' or 1:4 to 1: 5 'and can also be ι: 5 to 1:6. The thin film reactor is a device that can combine at least a chemical reaction with a thin film method or with a solid-liquid separation. In this way, the two programs can be integrated and synergies can be developed. Both programs can be housed in a single housing or device at the same time. During the chemical reaction, at least one of the chemical reactants is converted. By using a thin film reactor, the reaction product, intermediate product, secondary product, and final product can be selectively removed from the reaction mixture, and the precipitate can be added in a manner controlled by 201118162, or the reinforcement can be added to the precipitate. And the secret record, especially the water scale continuous reaction mixed σ removal. Therefore, a significant increase in production can be achieved. The medium or substance '_ is a decomposable oxygen-nucleus that contributes to the reduction of the anti-sequence and the rot, and the chemical heterogeneous changes in the domain, including the change in the density of the towel during the polymerization process, promote solid-liquid separation. By this, a higher solid concentration can be obtained in the reaction mixture. The reaction mixture is passed to a loop reactor depending on the amount of solids and the state of the conversion procedure. By this, the reaction mixture flows axially in the first direction and in the opposite second direction toward the axially inner cylindrical section. When a loop reactor is used, the inner tube can be provided with a heat exchange element to accelerate heat exchange and make the diameter of the reactor larger. The inner tube ^ is called an insertion tube or a catheter. The remainder of the catheter will affect the county power of the return and the loss of the deflection. When the length is constant, the deflection loss and friction of the reflow increase as the diameter decreases. When the selected diameter is too large, the reflow will collapse. The diameter of the insertion tube is approximately 1/4 to 1 直径 of the diameter of the reactor, and at most half of the diameter of the reactor. The conduit can be placed 1/3 or 1/4 of the base of the reactor. A reduction relationship (recjuctive reiati〇nship) is present in the reaction mixture. Due to the presence of an acidic environment, such as chr〇rine, there is a risk of corrosion of the surface in contact with the reaction mixture under operating conditions at elevated temperatures and pressures. Therefore, especially after a long period of operation, the wear resistance can be exhibited by local corrosion. Depending on the diameter that minimizes the action of the button, a rigidly mounted film member or a fluid-permeable cartridge can be used. The membrane element consists of a perforated element, in particular a metal plate that allows gas and liquid to pass through the element. Most of the gas-permeable cartidge is also made up of porous metal components. The purified propellant (pr〇pellant), solvent or water can flow into the reactor space. . When film components or fluid dialysis devices are used separately, they are not only related to the diameter and tolerance of the respective reaction vessels, but also to their form and corrosion loading. Plastics, metals, 201118162 hard metal, ceramic materials and polytetrafluoroethylene and especially stainless steel (stainless sted) and especially alloys for thin film parts are considered as possible materials, or The coating material is either a carrier material. The coating is usually not just a simple removable Teflon cartridge, for example on a laboratory scale, the device can be used in the form of pressure steel. Chemical, mechanical, thermodynamic and thermal methods can be used to apply the coating. To apply the material, the carrier material and/or the adhesive are thus presented as a gas, a melt or a solid. It is preferred to use direct current (Galvanic spraying or flame spraying), such as high-speed flame spraying (HV〇F). One technique that can apply a coating is electroplating. Instead of or in addition to electric ore. It is possible to arrange a cartridge in the inner space of one of the containers of the device. In particular, the inner wall of the reactor may be specially provided with a film member. The cartridge is mainly cylindrical and can be carried on the grid. On the grid, the grid refers to a mesh-like structure. Alternatively, the stainless steel casing is disposed on the outer or inner steel layer of the vessel or the cylinder H compared to the heat exchange panel system. Soldering in a point or f manner, whereby the unwelded area defining the fluid passage between the components or between the plates can be viewed or "pillowed" by the liquid ( Tempering Uquid) or heat exchange medium can pass through the fluid passage. Different media can pass through these cavities. These media can be used as heat, which can be fully added process water, light water, or steamed. Or hot oil. For y, the pressure load of the unrecorded steel casing (which is converted into the reactor space) is the most p, and the devices are used, and the pressure difference between the cavity and the reactor is as small as possible. A laser device is used in the hole to prevent or reduce the possible pressure difference in the cavity. Its :?| : 22, the form corresponds to the _ component or the tube 11. The separations are separated from each other as much as possible so that the media cover that reaches the reaction space may be small. 42 201118162 The distance between the holes in the casing or on the container is at least 10 cm to 2 cm, which may also be at least 60 cm and at least 150 cm. The medium is allowed to reach the internal reaction space via a hole in the inner reactor space or in the cavity between the reactor wall and the cartridge by an overpressure occurring in the casing loop. Laser joints are used to connect individual points or wire-welded circuits to create flowpassage, which ensures uniform distribution of the media in the housing. The pressure in the blending system exceeds the pressure in the reactor by up to 6 bar. The outer casing of the cartridge is directly adjacent to the inside of the pressure vessel. Alternatively, it may be adjacent to a perforated grid or a mesh structure. The cartridge includes regular pores having a diameter of from about 2 microns to about 70 microns. When an electroplated metal plate is used, an inner casing may be applied outside of the one-sided or double-side plating and/or after the occurrence of signs of wear, the body of which may be joined by soldering and preferably. It is connected by laser welding. At the same time, the cavity of the outer casing having the cartridge as described above can be formed for the use of the inner casing. The inner casing has a thickness of 1 mm to 1. 5 mm, it can be 1. 5 mm to 2 mm, or 2 mm to 2. 5 mm. The pressure loss is minimized and is further minimized by the size and number of input output nozzles. a cartridge made of steel or, in particular, stainless steel, or a film component, a reactor, a tube in contact with a medium, a heat exchanger or an accessory, consisting of steel or especially stainless steel, and used in the present embodiment Austenitic steels or grade 6, 7 and 8 steels of chromium and molybdenum or duplex steels (where German Industrial Standard (DIN) is 1. 457 Bu 1. 4404, 1. 4435, 1. 4539, 1. 4439, 1. 4462, 1. 4529, 1. 4501). In still further embodiments, more demanding reaction conditions are used, such as: copper, nickel alloys, high-key nickel-containing alloys, such as 2. 4610, and titanium. The wall thickness of the tube is designed such that the cartridge can be exposed to a pressure difference of 2 bar, in particular 4 bar and especially 6 bar. Especially in the base zone, there is a risk of agglomeration and blockage due to sedimentation and gravity. These hinder smooth heat exchange and deterioration. 43 201118162 The contact of precipitates in the reaction mixture hinders the control of the reaction. Therefore, the film components used in these partial injuries are specially processed, especially in the area of the substrate or the wall 'but at least in the conical region JL is preferably the lower 1/3 ,, in particular, deposition and knotation occur. The area of the block. These metal plates are treated such that they are drilled at regular distances on a metal plate, especially at distances below 1 mm, or below 6 mm and below 4 mm. Using a laser device to drill a hole in a component by a laser or a hole in the brewing hole, and having a straight (four) micrometer and a thickness of 1 micron, or between 100 micrometers It can also be between 50 microns and 25 microns between 2 microns. The hole is preferably flmnel-shaped so that the diameter exit of the hole is at least twice the entrance. By this, a fan-shaped flow is made to optimize heat transfer. The fine axial direction is almost parallel to the axial direction of the reactor and/or perpendicular to the surface of the perforated film member. The heated, cooled, and fully treated process water, fresh water, or water vapor is passed through the pores through the hole lions to the space of the pressure vessel, so that the holes can be condensed into nozzles. At the same time, the above-mentioned side of the new line is a blend and a propellant. Process water _ is that fresh water must be adequately treated so that it can be replaced by a hole/same or hot father. The target for the supply of water and the water of the container is for adjustment. "The cavity sealed by the internal space of the reactor is between the reactor wall and the membrane member as a guide for solvent, water or water vapor. The passage of the process water from the high hole is high enough. It can prevent the penetration of the reaction mixture. The strength of the film member or the wall of the cylinder is designed such that the strength of the wall completely meets the requirements of the difference in the force between the inside and the outside. The film or the cavity formed by the wall of the pressure vessel can be Divided into a plurality of regions, for example, contained in a cone or on the same surface of the base region. This feature is a unique pressure level. Different pressure levels are implemented, for example, by a valve or a separate pumping system. Thieves and agglomerates caused by the effect of gravity caused by gravity. The diameter of the hole adjusted by the resulting pressure gives a comparable effect. For example, the diameter in the region of stronger sedimentation can be larger. 201118162 Substituting The layer is either an additional substance that avoids the use of money, for the internal f-parts, especially the substrate or the pressure-capacitor and the base and other parts in contact with the reaction mixture, You can call the secret (4) (10) (4). This can be obtained especially by reducing the surface secret. Instead of or in addition to the surface treatment, the grinding method can be used after general pretreatment, which can be an electrochemical grinding method. Or it may be a % pole grinding of the metal in the electrolyte. The electrolyte is specifically related to the material. During the chemical conversion reaction, the energy contained in the raw material is close to 0 to 34% and is released in the form of heat. Go out. This energy is used by the heat exchange device to = the order of heat demand in the process towel. For example: it can be used to preheat the biomass or in the process or in the reactor or It is outside the equipment, this energy can be used to heat the room, machine or sputum as other process phase heat. Off (four) Lai lion, not only will, the chemical conversion program _ the ship, will also release the heat of the exothermic reaction = In this way, the development of the uncontrolled hot spot _ sp〇t) and the loss of the reactor can be eliminated, and at least one, preferably more, or a group of different harmonic systems can be eliminated. ,Electricity Or chemically driven. In addition, or take, instead of the process water system described in 'Taicho, the reactor's blending system, for example, the wall structure, screw-in radiator (screw_in radiat〇r), heating coil ^The coil is either made up of the (4) heat sink fins (fm) or the half-pipe line domain connected to the outside of the reverse wire. Instead of or in addition, the material according to the structure, the structure, and the Process water and/or hot oil is preferably used as a heat source carrier passing through and close to the internal space of the reactor or a blending medium for a blending system. Combination of individual blending systems , configuration, design and control are determined by the addition of engineering, especially according to the composition of the feedstock. All process water systems on the reaction side and in the reactor can be used to reconcile H on the other hand. Refers to the heat exchange process outside the reactor, and the other party, to reconcile the process water, such as for liquid jets or jet vacuums 7 & the desired materials such as for mixing devices, pumps and / or Dilution of the nozzle, 45 201118162 And, pumping medium or propellant. Mixed process water and fresh water are suitable for optimum reactor blending. Thereby, the processing procedure can be re-optimized by, for example, reducing the concentration of the specific inorganic substance. The introduced material is advantageously a blending medium, in particular a blending water or a recirculating process water that is critical in terms of temperature. The blending system is additionally controlled via a processing program. In addition to the combination of feed materials, pH sample preparation and catalysts, the delayed introduction of feed materials depending on the conversion characteristics is an important factor in temperature control. The process feedstock or reaction mixture viscosity, density and size, and other characteristics may vary during the course of the process. These changes are due to the &study and structural changes of the carbonaceous feedstock, which may also be the reason for the depolymerization and subsequent restructure of the feedstock. This, in connection with the machining process, creates different requirements for the mixing process. The mixing and/or fluid distribution is as uniform as possible, depending on the procedure, feedstock feedstock, solids concentration and demand for the reaction product. For the purpose of heat exchange and enhancement for the purpose of precipitation contact, and for the purpose of, for example, the cross-linked high-content lignin (Hgin) or cellulose (cdlul〇se) layer is more completely disintegrated, reactants and most For the purpose of the average distribution of the catalyst mixture and the discharge of the reaction mixture, agitation or suspension (SUSpensi〇n) is carried out in a continuous manner or in a batch manner. At the same time, the sediment decomposes, loosens, and eliminates embolization and condensation formation. The reaction is thus affected in a positive overall manner. This means that the more complete and uniform the mixing procedure, the faster the reaction proceeds and the higher the homogeneity of the reaction product. In the reaction space, a combination of at least one or several, and in particular different, mixing systems with and/or without moving parts can be used. In the reaction space, a combination of one or more or different agitators can be used as a mixture with movable components. The agitator is further provided with at least one and preferably two or more shafts so that more agitators can be driven by the same motor and reactor inlet. The relatively low energy requirement compared to the energy supply or compared to the mixing time is the advantage of this simmering system (10). In addition to the high cost, the main disadvantage is that it is easy to malfunction and high maintenance cost compared to the hybrid button in which the reaction empty towel does not have movable parts. Jet vacuum pump or liquid jet mixer (liquid 46 201118162 jet mixer) two pumps and nozzles (n〇zzle) are liquid injection systems "systems" These devices usually do not have any moving parts and therefore only need ^Less maintenance nozzle injection system can function as a mixing system, because it is suitable for introducing kinetic energy into the reactor via propellant, these propellants can also be used for heating or cooling, so as to facilitate The reactor contents are suspended or evenly liquided. The steps of the ruthenium include small size, minimization of flow and flow systems, and avoidance of the sealing system (sealjjjg SyStem). The streambreaker that is often used by the system is redundant. In the use of these systems, there will be no flow plate _ conditional fluid inactive zone (dead Z〇ne). At the same time, floating (floating of solids) is avoided, thereby reducing the risk of air intake. The liquid jet systems can be fed by a common or several process water reservoirs. These liquid ejecting systems can be controlled independently of each other so that different amounts of propellant and/or confluent can pass through the two materials, and it is better to have the propellant and/or the confluent ^ almost continuous / or called The way of closing is added. The neospray (10) system and especially the helium, the placement of the vacuum mill or the liquid jet mixer, is such that the liquid flow path is in the form of, for example, a vertical loop flow. The diameter_height ratio of the reactor is ’'back, and the flow is formed in the form of "8", or at a corresponding height, more = loop mechanical + lateral flow in the vertical direction. Liquid Mixing - or Jet The vacuum pump is preferably placed in the upper half of the reactor, especially in the upper third, whereby the jet of radiation is lying parallel to the axial direction of the reaction (4). Several (four) jet mixing: or squirting vacuum can be combined with a larger or higher reaction H in series, in particular, the control-height ratio is 1:3, which means that these are Not = degrees are connected in a (four) manner such that each subsequent mixing device re-accelerates the accelerated body. In the large diameter 'especially more than - metric diameter, several liquid jets are mixed with H or sprayed in a way that is set in the _ direction so that the spray is effectively applied at an age. If more than two liquid jets are used at a height to mix H or jet true H, the fluids of each of the several jet mixers will accelerate down to the base of the reactor. One or several liquids, jet mixers or jet vacuum pumps are placed on the conical or base area. The 201118162 square causes the fluid to be directed tangentially through the base or conical wall. - The number of her body jet mixing or the jet vacuum pump is placed in the conical bottom zone * next to the outlet nozzle so that the fluid passes directly through the base or conical wall in a tangential manner. Use (4) jet turbulence or turbulent flow of jet vacuum pump or f stress negative *^©@_(de_aggl() mer to hide the _ plus in the area where the turbulent flow and shear stress are the most loaded, especially It can be used in a predetermined manner to eliminate the formation of dumps and condensate in the sigma, subtraction or discharge opening, etc. In the position where the inlet and suction openings have a tendency to block, the turbulent water can be set. For the process, the process water only needs to be roughly processed for this purpose. For example, the Han selector, the filter and the ruthenium film are used for rough processing. Compared with the process water S of the propellant and the blend, the rough treatment is faster and almost straightforward. No or only a substantially low retention volume. Or 'into the inlet or suction opening of a convergent and dangerous mixer, away from its propellant flow loop and/or short-term flow reversal In order to control these nozzles, a flow meter (fl0wmeter), a pressure gauge (manometer), and a valve (valve) are used to react to the blockage by, for example, a change in pressure in the suction zone (short-term flow reversal mechanism). For pumping with clogging and sedimentation hazards The tank (sucti〇n sl〇t) or the suction opening, the mixed reaction mixture supply can be achieved by a split propellant fluid supply: one is directly absorbed by the reactor and the other is passed through The coarse filter is taken up by the upper part of the reactor. The propellant fluid supply is controlled and switched via a valve to save propellant, for example, when operational problems occur or when the degree of treated purified water is low. Nozzles can be used in the predetermined position of the internal space A. Among them, in particular, it is intended to prevent the dead zone or range of precipitation and agglomeration. 'Compared with the internal pressure of the reactor, there is continuous pressure in all liquid injection systems. Poor, to prevent the reaction mixture from returning to the mixer, pump and nozzle. Deceleration or retention accelerates the precipitation or settling of the solid reactants. It thus gradually accumulates in the lower part of the reactor. In the chemical conversion process, precipitates and agglomerates Will be formed in the reactor 48 201118162 iiiS (rrting) and the parts in contact with the reaction mixture. In the reaction = the inner grain is transferred to - After the mineral container, the actual operating temperature can be lowered. For example, the movable and controllable high mouth can be set. This clearing can be carried out under the control of the hand_continuation_, water room 2 or ίΐί. The cleaning device can use the force and temperature of far = f to get the best cleaning result, and the material is not. For the surface cleaning of the spray medium: Especially suitable: dry ice particles as the effluent are 300 per second. Metric (300m/s) 'and hits dirt with high kinetic energy = ir). Cool it to minus 8 (rc; the dirt layer shrinks and becomes brittle. ΐί ί 扩张 expands 700 times, making the dirt layer from the surface, set. The environmentally harmful organic solvent and the toothed carbohydrate step-determining advantage is Decomposition by dry ice particles in the air becomes redundant. Dry ice blasters are preferred & ^_ve_kelsystem. The dry ice blaster is introduced into the reactor through a hand hole at the = position, and leans into the previously set holding system to dry the granules by rotating the scatter device (4). Liquid or helium gas medium such as water, reconditioned or treated process water or gas such as water vapor can be used as a propellant for jet vacuum pumps or liquid jet mixers. * When the yarn is in the middle or just after the process, the process is screened, alkali and lining impurities, so that the mixing device, the chestnut and the nozzle are not blocked, and the wear of the H-tube and the other base of the hybrid can minimize the temperature of the agent. The Wei line adjustment makes it guide the rib to control the temperature. The push/tune media is passed through the outside of the reactor at a pressure equivalent to the reaction!! (10). If the process of the process water blending system has been lost, the propellant/conditioning medium will pass through the outside of the reaction at the temperature of the reactor_fluid phase #. Replace process water 'fresh water, steam, or water from other processes

C 49 201118162 Used as a propellant, heating or cooling. The materials in the process water are related to the mixture of feed materials and the processing procedures including the catalyst. Materials that are previously associated with biomass are broken down by procedural fragmentation. In the chemical conversion process, many elements include gases, sulfur, nitrates and their salts and metals, especially heavy metals and inorganics, and alkali metals such as potassium or sodium and alkali metal salts enter the aqueous phase in some parts. Part of it is combined again in the solid phase. The remaining part is retained in the liquid phase. The portion of the material that is combined with the liquid phase is also related to the difference in concentration, which is the concentration that has been exhibited in the liquid phase. Achieve some ugly precipitation and increase in concentration under the Wei. The acid and the compound are sour and chloride can precipitate as a salt and thus adversely affect the processing procedure in the reactor assembly. In the liquid phase, the portion of the organic carbon compound is 50 grams or more per liter. The chemical 〇xygen demand (COD) of the process water without recirculation has been higher than 5 mg ο, which clearly exceeds the statutory import limit. One ▲ understands that chemical oxygen demand (CQD) is the amount of oxygen required to chemically oxidize the organic matter content. There is / depending on the moisture content of the feed material and the processing procedure including the solid-liquid ratio, and the process water part of the loop is 35%, or 35% to 6〇% or ^ It can be 6G% to 85%. The production of money is almost completely back riding, which means that the system, the water loop or the restriction is only possible in a limited way to save fresh water and reduce the volume of wastewater. In addition to the accumulation of organic carbon compounds, a large number of inorganic materials such as sulfides and compounds such as sulphide are concentrated. The concentration of inorganic impurities accelerates as the lime deposits in the reactor can interfere with the flow of impurities such as pumps, valves and nozzles. Thus, the sulfate that increases the reactor design will precipitate. The cumulative time-saturation time is related to the material composition and processing procedure of the feedstock. The conversion process usually lasts for hours. During this time, the material of the lion is in charge of 'required test _ these, so that the first two to three program stages of the addition process ίίί Γt provide a variety of different (four) i L minus expected reaction products in the interval - for example, near the end _ Program stage ~ bundle to recover the reaction product. Retrieving propellant during the process of the process 50 201118162 or blends such as gas, water, are process water and / silk gas / synthesis gas and catalyst. The reactants and especially the secondary products that will disturb the chemical reaction, mixing and flowing processes are removed. Different methods are available for the deposition of solid materials and especially for the reaction products in the reaction mixture. The solid-liquid separation is used for the separation of the liquid phase, whereby the body can be obtained and concentrated. Different screening procedures (coarse screen, fine screen), filtration procedures, and/or deposition by centrifugal force by cyclone can be combined with each other for separation of solids. In order to reduce the burden of filtering or screening during the process, one or several filters or filters are performed in the scope of the pre-processing. By these two methods, at least one coarse filter or one fine filter or both can be implemented. The amount of 1/3 to 2/3 of the total organic carbon compound can be removed from the process water by filtration, particularly microfiltration and/or ultrafiltration or a combination of the two. It is preferred to carry out the solid-liquid separation under the operating conditions, and usually not only using a simple filter paper such as a laboratory scale. The choice of method of use depends on chemical composition, particle size distribution, density, particle form, hardness and solubility, etc., and includes the use of current and load, different densities and centrifugal forces, and different particle sizes. Dynamic, static, vacuum, pressurized and sterile filtration, among which cross flow filtration includes some of the available microfiltration, ultrafiltration, nanofiltration and reverse osmosis systems. . Preferably, a device utilizing a hydrocyclone, a centrifuge, an electronic or magnetic separation device and/or a filtration method or a functional principle is used. Among them, the preferred filtration method is particularly suitable for use in the reaction conditions of hydrothermal carbonization. For solid-liquid separation, it is preferred to use a rotating disk filter, centrifuge or centrifugal membrane transition device under operating conditions. For the formation of holes, the material is preferably made of metal and especially ceramic. The form of the porous forming material is preferably a disk shape. The size of the pores of the filtration device and the amount of solids in the filtrate are not always proportional, depending on the filtration method employed and the material being introduced. This is especially true for the use of ceramic materials as filter elements. The aqueous phase is introduced into the process water reservoir in a filtered or unfiltered manner. The nature of the solid to be separated, and the selection of 51 201118162, the method of separation is based on the processing procedure and the characteristics of the desired reaction product f. The deeper the procedure is, the higher the density of the reaction product, and the easier it is to complete the procedure. Recorded the suspected condition τ. The solids content in the face fluid typically sinks in proportion to the size of the pores and can be significantly increased by over the use of hydrazine and can exceed 2/3 to 4/5. Integrating one or several solid-liquid separation devices into a process for removing sediment or other impurities having a high density or a high weight, which can be separated by centrifugal force separation during the treatment of the biological f The use of the principle is particularly advantageous for the cleaning of process water, which acts as a propellant spray medium to protect the pump, mixer and nozzle. During the procedure, the process water is re-adjusted from the upper half of the reactor, especially from the top of the reactor, preferably by one or more of the 1/4 points above the reactor. deal with. The re-adjusted or treated process water is returned to the water loop of the equipment for recycling. One less and especially several processes ^ The reservoir can be used in several reactors for each-face-reactor. The different cleaning steps are performed in separate process water reservoirs. The capacity of the individual process water reservoir or the shared process water reservoir is approximately 35% to 85% of the total volume of the reaction H. The process water is stored, the temperature of the device and the Lili load are designed to make the pressure drop. The degree and heat exchange device are not available. - Process water cleaning is integrated into the water loop that it is prepared for. The difference = processing or re-machine method depends on the system of re-adjusting the program water. Different t chemical and biological methods and devices are used for this side or in combination.

Aerobic and anaerobic high-performance bioreactors (anaerobic high perf__ biQ biofilm reaction 1 (biG membrane m s), anaerobic and animate sluny meth〇ds. The above water cycle should be comparable To reduce the content of organic matter in the jujube, but it is necessary to measure the amount of organic matter and the alkalinity of the organic matter and the concentration of the inorganic material in the returned process water; (such as calcium). In order to recover as high as possible Part of the process water is a particularly effective combination of the same method and device. The agricultural system used for mechanical waste water cleaning is a filter, preferably a microfiltration 52 201118162, and especially an ultra filter, and is applicable. In the above-mentioned solid-liquid separation method, the solid-liquid separation device in which the magnetic H is established is preferably a rotating disk filter and, in particular, a fine water or a wastewater. Clean, 疋 use - a device that 's quick to meet the needs of cleaning or handling complex. For example, it is best to use a device with a steel structure, such as a high-performance bioreactor in a biofilm process, preferably Oxygen process water treatment, especially one-circuit reactor. In this design, the loop reactor is designed with an effective nozzle to mix the solid and liquid phases. Instead, or for the aerobic method, for the anoxic method. Oxygen process water treatment reactors or reverse dectrodialysis can also be used, especially for the recovery of nitrates, distillation, evaporation and/or ion exchange processes and activated carbon. Odor exposure causes solids The need for storage and transportation and the design of equipment, buildings and conveyors. The intensity of ozone exposure will decrease with storage time. Buildings or storage and transportation spaces, especially for fuels, are designed to be impervious. Or impervious to ozone, so that the air carried can not be dissipated. The passage of the building is sealed by the gate. One or several chemical and / or biological air cleaning equipment is provided, so that ozone exposure can be reduced for employees, suppliers and residents. To a minimum amount. The cooling of the reaction product, especially at an absolute pressure of 1 bar below the boiling point temperature, Externally, it can also be carried out in a device for liquefaction jevolatihzation). The heat energy thus released can be used for other procedures via the heat exchange program. One or several grinding steps can be carried out before the cooling of the reaction product, during the cooling process, or after the cooling. It is preferred to use a mill or crush 2 generation. The separation of the solid phase from the mixture is usually carried out mechanically in the first step in a first step in a thermal separation device.曰 Use a static thickener to reduce the water 重力 'with or without a mechanical rotating device or a raking machine, for example 53 201118162 ©^AmH(stationary thickener)(through device (dosing device) Control the supply. This material device can evenly distribute the concentrated mixture and can be directly integrated into the dry county with the corresponding high volume = several machines H. The conical structure is superior to the Wei scale and can be a direct rail mixture. Corresponding to the quantity? Adjust the equipment of the shouting part. Or you can also introduce the mixing to be concentrated into an isolated sieve surface or a curved selection (CUrVed SCreen). Centrifugal force squeezes a part of the liquid through the slot of the j-selector. The mixture process is finally sent to the dry attack. A hydrocyclone provides a more favorable separation method, in which the solid and liquid systems are separated by ~ Accelerate to separate. In the submerged flow (dump 〇fl〇w), it should be concentrated to the county, and the treated or purified liquid leaves the hydrocyclone in the overflow [by the front and adjusted concentration And The dosing device is inserted to ensure continuous and optimum supply to the drying device. It is particularly important for the drying of the shearing centrifuge. The shearing centrifuge has high operational safety and is suitable for use. Dehumidification and cleaning of granular solids. In addition to the mechanical means that must be connected before drying for energy reasons, it is preferred to use a thermal drying method. The amount supplied to the drying process is greater than one kilogram. Continuous The operation is preferably for a filling operation (charge 叩 〇 〇 。 。 。 。 = = = = = = = = = = = = = = = = = = = = 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 A correction drier is used to dry the reaction product as well as the secondary product, whereby the material to be dried is contacted with the hot dry gas. The disadvantage here is that the gas used is to be discharged, and usually requires a dust separator ( Dust separators). The gas may scream humidity after condensation. For example, a fluidized bed dryer can be used as a pair of flow dryers. Or what you need _ grain size ^ use spray ^11, nozzle tower or H money machine (fl〇w drag disk noisy), drum (d_) or wear drier (tunneldrier) The continuous procedure is advantageous. 54 201118162 μ When using the contact type, basically only the turning surface can be used for the heat total belt, vacuum belt, drum (dmm), heart dscrew ), Cyiin (jer), drum type (four) (four) or belt dryer ^dt, in particular, the use of a vacuum drum filter (vacuum drum 1 ter) or dryer. In order to obtain a lower moisture content, depending on the yield, a disc dryer (disk sink) may be used selectively or additionally. The drying procedure is carried out by means of a h〇t gaseous medium, such as air J: fullness. Between 6 and J machines, preferably between hungry and sturdy, ^gui: between 7〇C and 85°C. Instead, overheated water vapour is used in all of the above thermal drying devices and particularly preferably at a temperature of 130 ° C to 18 (TC steam). A combined mechanical-thermal method (mechanicai - Thennai meth〇(j) can be used for separation or reliance. Compared with the reading method, the surface-heat method has the advantage of having a significantly lower residual humidity, whereby the product can be transported or transportable. It is improved, especially with fine particles or a product of the nano system. A further advantage is that some of the contaminants in the reaction product are washed away by condensing steam. The use of steam is further driven. The dehumidification enhances the efficiency of the centrifuge operating in the filtration mode. The mechanical displacement mechanism of the condensing tip cooperates with the inertial force to cause complete consumption of the capillary system which actually causes the coarse slit. In these methods, for example, steaming Gas pressure filtration uses this mechanism. It uses saturated or superheated steam to remove the gas pressure difference instead of using pressurized air. In particular, in a method space, according to the present case, in combination with the process of vapor pressure and centrifugal dehumidification, the finely dispersed solids of the reaction product are transferred from the suspension to the final product of drying, purification and free flow (free Flowing end produei) The residual moisture content of the reaction product according to the present invention is advantageously about 6 〇 /. to 25% 'may also be 10% to 20% or may be 12% to 15%. After the conversion reaction' The reaction mixture is presented as a suspension, wherein the structure of the subsequent reaction product, intermediate product, secondary product and/or final product is related to the feed material. ' 55 201118162 The classification of fuel is made by coal (peat-like) , all lignite-like to coal-like fuel (coal-likefbel), humus, Maynard or Maynard-like reaction products, carbonaceous materials such as thermal insulation materials, nano sponges, pellets a carbonaceous material such as a pellet, a fiber, a cable, an active coal, or a sorption coal-based material or a charcoal substitute material. Highly compressed carbon products and materials' and in particular feedstock materials for graphite and graphite or graphite-like products, as well as carbon fiber and composite feedstocks and flber composite materials. According to the present case, 'pure, The purest and ultrapure coal-based materials are products. The advantageous properties of these materials are mainly due to the reduction of mineral matter compared to the feedstock. Pure coal is mainly understood as the combustible part of coal, and the purest coal is also understood to be active coal or charcoal. The mineral content of the ultrapure coal is, for example, less than a weight percentage of 0.1. Figure 1 shows a device 1 with a reactor 2. The reactor 2 is composed of a cylindrical body 3 having a reaction space 4. The reaction space 4 is used to contain a solid mixture such as biomass. Reactor 2 contains a filler 5 and an outlet branch 6 for the solid-liquid mixture, from which the intermediate product, secondary product or final product can be removed from the reaction space 4. Its reactor 2 further comprises means for mixing the solid-liquid mixture. In this embodiment, the mixing device is shown in the illustrated transfer device 7' where the treatment and/or processing of the towel can be mixed by solid-liquid mixing. The reactor 2 further comprises a cylindrical conduit or insertion tube 8 which directs or controls the flow of the solid-liquid mixture in the reaction space 4. And the numerator 2 also contains a - 妓 妓 赖 儒 ^ ^ ^ mixing device. The reactor 2 is further provided with a filter device 1 by which the body composition remains in the reaction space 4. The process water or industrial water can be retrieved from the reaction space 4 and sent to one via the filtration unit 1 and the line u. The water can be supplied to the Confucian or liquid jet mixing °°, thereby being sent to the solid-liquid person 3' in the reaction space 4 via the line 1 or can be used as a clean water guide through the finer 14 - a storage ^ ^ mouth. 56 201118162 Purified or treated water can be stored separately! ! 15 is returned to reactor 2 via line 16 or to wastewater via line 17. Figure 2 shows the basis according to the first! A cross section of the wall region of the reactor 2 of the drawing. The reactor wall 20 is formed as a double wall, and the reactor wall is composed of an outer wall layer 21 and an inner wall layer 22. The inner wall layer 22 is at the edge of the reaction space 4, and a membrane part 23, which may be a perforated metal piece or a thin film metal piece, and is a heat exchange plate. The film member 23 may be mounted in the reactor 2 or may be attached to the inner wall layer 22 by soldering. The outer wall layer 21 and the inner wall layer 22 have a distance from each other such that a cavity 24 exists between the outer wall layer 21 and the inner wall layer 22. In the heat exchange apparatus, hot oil may be present in this cavity % as heat energy transfer. The hot oil is heated and the hot oil is introduced into the cavity to heat the internal space of the reactor 2. This is done in a closed loop. The advantage of hot oil over water is that the hot oil has a significantly higher boiling point and can therefore reach 300. (The temperature: there is another 25 between the film member 23 and the inner wall 22. This cavity 25 is for accommodating clean water and can be used, for example, as a blending system. If the film member 23 is a film metal sheet or a perforation The heat exchange plate, the pressure in the chamber 25 needs to be at least slightly higher than the pressure in the reaction space 4, so that no components of the reaction mixture can reach the cavity 25. Due to the extreme reaction conditions in the reaction space 4, the inner wall 22, Mainly the film member 23, which is composed of a corrosion resistant material or at least coated with a silver resistant material. Fig. 3 is a schematic view showing an example of an embodiment of a device. The combustion of a fuel or a reaction product produced in the device, according to the fuel The type 'is carried out, for example, in a pellet burner (pellet such as (10) (3)), a pellet vessel or an additional combustion device, preferably with an automatic fuel supply. The configuration for energy generation may, for example, comprise a combustion The form and size of a combustion disk in a pellet burner is adjusted to ash c。ment. According to the invention, due to the use of the device The lower ash 'small burner disk size is sufficient. To prevent agglomeration in the combustion disk, the combustion apparatus or the pellet burner according to the present invention is provided with an automatic device 57 201118162 for removing ash from the combustion disk. In the process of generating energy in a dust-like fuel (dust-like fUel), the dust burning device according to the present invention comprises a coal-fired power plant or a pulverized coal combustion with at least one steam turbine or supercritical Supercritical coal-fired power plant. In order to achieve high efficiency 'the combustion procedure is carried out at temperatures as high as possible above 600 ° C, or exceeds 650 ° C ' and in an example of another embodiment Its temperature system is more than 7 〇〇. 〇. Further use of modern power generation equipment technology to increase the efficiency in high temperature areas, so that the current production can achieve the highest possible efficiency of the gas steam turbine program 'system performance up to 43%, or more than 46%, or in the further examples, the example is 49% to 55%. Using integrated coal enthalpy gasification technology The integrated gasification combined cycle (IGCC) is suitable for the combustion of fuel produced according to the method of the present invention, and the fluidized bed combustion technology can also be used, in particular, the fluidized bed double cycle power generation technology (PFBC) and especially It is a combustion power generation equipment with a combustion coal gorge recirculating shield ring energy such as pressurized pulverized coal combustion (PPCC). ^ The combustion procedure should have a higher than 1000. (: The fuel intake temperature, preferably, is 12 GG ° C, and particularly preferably higher than 14 G0 ° C. The fuel gas removal system at high temperatures is designed to utilize the low temperature plasma characteristics of the fuel gas to make the particles The content of the content and the corrosive substance, in particular the sodium and potassium compounds and the corrosive fuel gas, are reduced to such an extent that the fuel gas can be immediately sent to the gas turbine. According to the present case, the liquid slag for the fuel gas is provided in the apparatus. The separation device can achieve a particle content of less than 3 mg/m3 in, a diameter d of less than 3 μm, and an alkali content of 0.01 mg/m3 in. Another way to generate electricity or energy from a dusty fuel is to use carbon fuel. Carbon fbel cell. Compared with hydrogen fuel cell, the fuel cell has two distinct advantages. In other respects, the carbon is charged twice as large as the hydrogen molecule. The volume of the milk before or after the reaction has the size of the marriage, but the hydrogen tank battery is different in the two condition volumes 58 201118162. This means that the entropy of the former is hardly changed, therefore, The fuel value can be completely converted into electrical energy. The utilization rate of the carbon fuel cell can theoretically be higher than that of the hydrogen fuel cell by 60%. To obtain the required carbon particle density is a "challenge. According to the equipment provided in this case. The particle size is the possibility of a coal-based fuel for the nano range of carbon fuel cells. The synergy with other energy-generating methods can be established by using a common energy generating device, in particular a turbine such as a steam turbine, for example Gas used in wind towers or wind turbines. Dispatchable Wind Power System (DWPS) is the most commonly used turbine and especially steam or gas turbine in these renewable energy sources. The depressurization is carried out in a plenum chamber. The efficiency is increased by more than 20°/. to 200°/. or 40% to 170°/ by the introduction of compressed air into the turbine. Another example in the embodiment is an increase. To ι5〇%. According to the present invention, the energy generated by the use of the generated fuel in the device, in particular in the form of heat and/or electric energy, at least Some may be one of the following designs: • distal and proximal heating networks; • feedstock, water (including process water), reactants, intermediates, secondary products, and/or final products, particularly fuel, Processing and processing procedures for Maynard or Maynard-like reaction products containing carbonaceous materials, humus and/or biomass, including grinding, drying, dewatering, conditioning, removal of metals and impurities, and/or drying^ In particular, metal-containing substances, such as by cyclone separation devices, perturbations or mixing systems, pumping, heating, steam supply, heat exchange procedures, compression, transfer and transfer procedures, process water, water And wastewater conditioning & treatment and air cleaning or treatment, solid-liquid separation procedures, cooling and adjustment for further procedures and energy regeneration. • Industrial operations for the production, processing and processing of metals and foods, especially for metal, especially for crushed iron, food, especially for milk processing, wine processing, greenhouse or non-greenhouse gardening, and meat processing. • Operation and production operations for fertilizers and fertilizer tools, tire recycling 59 201118162 Tire recycling plant operation. • The operation and production equipment of the chemical industry, especially the processing and production of air and other substances in gaseous or liquid form. Other substances include oxygen, nitrogen and argon. • Water cleaning and desalinization plants, especially using reverse osmosis; or • oil mill, refinery, ethanol production equipment. For heat and energy exchange and for synergistic potential, the utilization of fuel and/or reaction products produced by the apparatus according to the present invention can be operated with different power equipment and energy generation programs. To this end, the following applies in particular: coal-fired power plants, in which integrated gasification eombined eyde (IGCC) and fluidized bed combustion technology, especially Circulating pressurized fluidized bed combustion combined cycle (PFBC) and in particular combined energy equipment and coal-fired anti-combustion cycle, such as pressurized pUiverized coal combustion (pressurized pUiverized coal combustion (pressurized pUiverized coal combustion) PPCC) • Gas power plant; • Fuel cell with different fuels whose fuel contains methanol, coal, oil and gas; ' • Biomass power plant; or • Solar power A solar power plant. Figure 3 shows a device for energy production with a device 1 for processing biomass and a configuration for energy generation 2. The device 1 comprises two reactors 3, 4 Connected in series, each having a cylindrical body containing a reaction space 5 and acting in the form of a pressure vessel. The space 5 serves as a feed material for containing biomass. The apparatus further includes a grinding device in the form of a chopper (Pong) 6 and a mill 1) 7. The biomass is first supplied to the shredder 6 for coarser grinding (as indicated by arrow 8) and then to the mill 7 for further grinding. The raw material 201118162 prepared in this way is then concentratedly mixed in the mixing device 9, whereby an auxiliary material such as a catalyst can also be added (as indicated by the arrow ίο). The biomass is then supplied to the reactors 3, 4 via line 12 by means of a pumping device apparatus 11 and further at a pressure of, for example, 7 bar and for example at least 16 Torr: <Processing in reactor space 5 at elevated temperatures. The adjustment of the required temperature in the reaction space 5 is confirmed by the blending system 13. The blending system 13 may, for example, comprise means for applying a cold head, which is supplied to the reactors 3, 4 or reacted by heat exchange with a pump 14; The biomass feed into the continuously arranged reactors 3, 4 is controlled by valve means (v = ve device) 15, 16. After the biomass treatment, the reaction product is taken out from the reactors 3, 4 and supplied to a separation device 20, which separates the solid reaction product from the liquid component. The liquid components are supplied to a waste water conditioning plant 21 and cleaned in an environmentally compatible manner. The still moist solid reaction product is sent to the drying unit μ via the liquefaction unit 22, and these solid reaction products are dried to the desired residual moisture content. The dried reaction product is typically pulverized coal or a similar fuel. The fuel is temporarily stored in the force-fuel reservoir 24' which is disposed between the device 'and the configuration 2. The configuration 2 for energy generation comprises a combustion device 3〇 for burning the fuel produced by the device 1. The heat of combustion is used to burn the apparatus 30 for heating, or to generate water vapor in the tube member 31, and to drive the turbine 32 by the steam generated by the method. The rotational energy of the turbine 32 can be provided to a generator 33 and thereby converted to electrical energy, which can for example be sent to an electricity network (as indicated by arrow 34). The fuel gas generated during the combustion of the combustion apparatus 3 is discharged to the open air via chitoney 36, and is treated by a cleaning method 35, which includes, for example, a desulfurization of a fuel gas and a Fuel gas NOX removal device. The organic material and the inorganic material are removed from the feedstock during the process or during the chemical conversion process and are therefore available for use and easy to access. The improvement in availability is partly due to the previously difficult to obtain or partial decomposition of the chemically bonded material. The extent of its occurrence is related to the reaction or treatment strip 61 201118162. In addition to organic decomposition and undecomposed substances, inorganic substances such as alkalis, metals, salts, and acids, calcium, magnesium, gas, iron, aluminum, and phosphorus containing humic acids: bells, nanoparticles, nitrogen, and their compounds also belong to Remove or use materials that are easier to take. The solid carbon component of the reaction product appears as a material and/or fuel after the conversion reaction and has the following characteristics, wherein: the composition of the material and/or fuel can be controlled by a reaction procedure. The concentration of individual materials cannot be arbitrarily changed immediately and independently of other materials. However, different material groups and parameters can be changed in the same direction. For example, in the low-sulfur content of the city, chlorine and ash are simultaneously reduced. By elemental analysis of different measurements of 'grass, cut hedges (thuja) and sugar beets, elements with a carbon content of more than 50% to 63% (dry mass) The percent mass fraction, and thus the mass fraction of the feedstock, is from about 20% to about 60%. The oxygen fraction was reduced to half and the nitrogen fraction was about 1/4 and the hydrogen fraction was reduced to about 1/4. Compared to biomass, the carbon content of materials and/or fuels increases by 1% to 300%, and may also be 50% to 3% or 1% to 3%, especially 2%. Up to 300%. The carbon fraction of the fuel and/or material is increased by 5% to 20 〇G/°, particularly 10% to 150%, particularly preferably 10 to 120%, especially 50%, compared to the feed material. % to 100%. The carbon content of the feedstock and/or fuel is usually between 40% and 95%, and may also be 50. /❶ to 鄕, or 55% to 80%. Depending on the reaction procedure and the feedstock, the carbon fraction can also be higher than 98°/〇. The hydrogen fraction of the fuel and/or material is reduced by 1% to 300%, 5% to 200% or may also be 20% to 1% compared to the feedstock. The oxygen fraction of the fuel and/or material is reduced by 1% to 300%, and may also be 5% to 200% or 15% to 1% compared to the feed material. The nitrogen content of the fuel and/or material is reduced by 1% to 300%, may be 5% to 200%, or may be 15% to 100%, as compared to the feed material. 62 201118162 The sulfur content of the fuel and / or material may also be the fraction of biomass and may be reduced by 1% to 300%, may also be 5% to 200% or 200% to 600% or compared to the feed material. It is 400% to over 1800%. The ash content of the fuel and/or material may be a fraction of biomass and may be reduced by 1% to 100%, or may be 101% to 1000 Å/〇, or may also be 1000% to over, compared to the feed material. 3000 〇 / 〇. The particulate matter relative to the feed material 'fuel and/or material may also be a fraction of biomass and may be reduced by 1% to 200%, may also be 201% to 1500%, or may be 1501% to 2000%. In the combustion process, the high content of the process water can be used to reduce the inorganic materials and the ash and fine dust fractions, for example, up to 3%. The above fractions of matter and the dilution of various other substances occur by an increase in the proportion of process water. These materials were originally contained in the feedstock and were removed and decomposed during the conversion process. It can also be said that these substances are washed away so that the fraction of soluble substances can actually be reduced according to the proportion of process water supplied in the solid phase. = Even if the catalyst composition is not considered or the suboptimal reaction conditions are dominant, a higher carbon fraction can still be obtained, which exceeds the carbon content of the feedstock by 5% to 10^. Proper handling and processing of biomass can range from 55% to 77%. Carbon fraction. In a suitable processing procedure, a suitable feedstock comprises an adjustment of the catalyst mixture to obtain and above the amount of carbon. These values can be compared to fossil fuels. After the end of the conversion reactor, the carbon fraction of the material and/or fuel has indeed increased 'but the energy content or fuel value has decreased by 36%. Because of the release of heat in the reaction, it is an exothermic reaction (drinking is also 6〇11311^(^〇11). On the opposite side, at least 65% of the raw biomass of the dry biomass is related to the mass of the feedstock. β If a carbohydrate-containing biomass such as grain, corn or sugar is used as the feed material, the fuel value of the material and/or the fuel value of the fuel is about 65% to 85%, in another embodiment In the example, compared to the feedstock, 63 201118162 is 7 ()% to 8G% °. The less carbon hydration in the feedstock, the lower the energy of the cap during the conversion reaction. The second raw material, at the same time, the higher the fuel value of the reaction product. Depending on the biomass used, the energy of the reaction product is as follows: if the lignocellulosic biomass such as cut and leaf is harvested or harvested as feed The conversion of the raw material 'the material and the domain fuel is about 7 ()% to 9 %. The mass of the starting material is related to the weight of the starting material, which can also be 75% to 85%." If it has low carbohydrate, cellulose or wood quality For example, clear money is the fuel value of the sewage county as a scale. 95%, with the quality of the starting substance J "can also be 85% to 90%. Pure, most critical or super-sense (10) shirt as a chemical substrate and secrets, 1 scale - step weep = carbon fuel The fuel in the battery. 4疋 and biased material f in the reaction process from the solid phase decomposition into the water phase and appear in j water. Most inorganic substances such as phosphorus, sulfur and nitrate can be processed by the process = back. As a fertilizer, a raw material or a material in other processes. In order to ensure natural circulation, the inorganic component may preferably be separated from the liquid phase to return to the surface for the natural development of the biomass. The raw material extracted from the biomass = the nutrients contained in the surface of the rainbow, the aeronautical can be transferred - close to the closed cycle. The polymerization by depolymerization (10) reading and learning carbon compounds and structures. The condensate formed therefrom can be ground by a lower energy input than most known solid fossil fuels. Further, brown μ < m-form_(tetra)ϋ is based on the feedstock, perhaps due to the formation of the Maynard reaction product. Many of the feed materials have a lower density than water before the reverse. The density continues to increase during the course of the reaction. Depending on the feed replenishment and the reverse order, 64 201118162 achieves a density comparable to that of black coal. When the density of most of the feed materials is between 2〇〇kg/m3 and 600kg/m3, and the density occasionally reaches 8〇〇kg/m3 (dry weight), the density of the reaction product can reach more than 9〇〇kg. /m3 to 12 〇〇kg/m3, and occasionally also reach 125〇1^/1113 to 135〇kg/m3, which is assumed to be that air between the particles of the reaction product is removed or by extrusion. By virtue of the small particle size of the reaction product, a larger surface area is created compared to the feed material. This results in easier drying at the same moisture content than naturally occurring carbon compounds containing a comparable amount of carbon. At the same time, the large surface area contributes a lower ignition temperature. The unique properties of the reaction product are found in Maynard or Maynard-like reaction products and in liquid and solid phases. Strong odor formation changes with the feedstock. Basically, the formation of odor is related to the formation of the Maynard reaction product. It has improved conductivity compared to other carbon compounds which have a comparable amount of carbon. • Peat to black coal fuel. • Less volatile than conventional or fossil fuels of the same carbon fraction. Dan. Combustion produces lower ash, lower nitrogen, sulfur, nitrate, heavy metals and reactive substances, ie lower auto-ignition temperature than fossil fuels with the same high carbon fraction. . • The composition of the fuel gas is favorable and has less damage in combustion than in fossil fuels with the same high carbon fraction. In summary, the characteristics of the new reaction products described above, as well as their environmentally friendly and friendly properties, can provide a number of advantages over conventional fuels. Compared to traditional biomass energy recovery, it is more efficient and economical to process for biomass-based materials and/or fuels. In the biomass conversion paper, there is almost no carbon loss. More than 95% of the carbon in the feed material passes through the solid component + which enters the reaction product, which can be converted into energy. The surface of the carbon compound becomes liquid 65 201118162 ==:3⁄4: The matter is about 1%_4% of the carbon-based ruthenium phase in the raw material. The fraction and the liquid s carbon of the ageing material are formed by the anti-filament county, and the f is formed by the domain and surface of the feed and the recharge. The material part is the material used for 2 and the surface clarity. In these #, for example, a nano sponge can be used as a reservoir for water or as a barrier material. - The Meiner reaction of the households in the heating process such as protein, protein-containing and carbohydrate-rich foods at temperatures above 13 (rc baking, fry, roast, grilled (gnu) and fried During the so-called Maynard reaction, red to yellow-brown, sometimes black, brown spots (melan〇idines) come from scented flavor enhancers as well as carbohydrates and amino acids. Especially many black The browning is formed at high temperatures during the baking and roasting process, but the reaction is also accelerated by more than two pressures, whereby these form part of the product in the product, such as bread, Coffee, malt, nuts or corn flakes and, for example, coffee that is increased to 30%. In a first non-enzymatic reaction (non_enzymaticreacti〇n), the feed precipitate of the Maynard reaction forms a Schiffbase This step is performed in a few minutes or as long as several hours and is reversible because the Schiff field is a very unstable compound. The amount of the Schiff field is directly related to the concentration of glucose, when glucose is shifted from the reaction. Divide or At lower concentrations, as the product decays within a few minutes, the unstable Schiff field is further converted to a more stable product of the Amadori (Amadori). This procedure is significantly slower, but It is more irreversible, and the Amadori product will accumulate. The initial Amadori product will rearrange itself and further react to the final product reaction of the Maynard reaction, which is the highly glycated end product (advanced glycation end) Product, AGE). Highly thiolated final products can be crosslinked with other proteins via rearrangement and polymerization. Due to the developmental pathway, there are many different and complex forms of highly glycosylation. The detected forms are Νε-(carboxymethyl) lysine (CML), glycosine (fUrosine) and pentosidine. Maynard or Maynard-like reaction The product is formed at a high concentration during the hydrothermal carbonization process. There is a relatively high concentration of indicator CML in the solid (between other solids) and in the liquid phase (eg process water), usually at a concentration of 0.3-2. Mmmol/ mol lysine. Generally, the concentration in the liquid phase of the reaction product, that is, in the process water, is higher than that in the solid phase. The concentration or concentration ratio is based on the solid-liquid ratio and the composition of the feedstock. Determined by the processing program. Antioxidant and chemo-preventive properties are assigned to CML, which assumes that other intermediates, secondary products, or other products in the hydrothermal carbonization process can be compared to similar or similar properties. The reaction product is found in the Maynard or Maynard-like reaction product. The Maynard or Maynard-like reaction product is isolated by filtration, ultrafiltration and/or chromatographic methods, in particular by column chromatography. The humus produced by the hydrothermal carbonization process according to the method of the present invention has a relatively short residence time compared to a reaction product having a higher fuel quality. It typically still includes the fibrous material of the feedstock (which contains lignin and cellulose). The biopolymer is not completely depolymerized. The humic system formed according to the present invention has a carbon fraction of at least 30% to 45% and a calorific value of at least 15 MJ/kg to 24 MJ/kg and is easily burned. The humus produced by the method according to the invention may have some properties similar to those of natural rot, and some may also have characteristics similar to peat or peat: • protect the land from rainwater, since the water may be uniform and Deep penetration; • Reduce wind erosion; 67 201118162 • Amazing food worms and other useful soil organisms; Lowering land temperature in summer and increasing land temperature in winter; • Supplying nutrients to plants, nutrients Slow release, so that plants can be treated; Quantity; · Make the land can be stored in the county, 纟帛i water and limit the fiber to a minimum process by adding lime and organic fertilizer to make a chemical change in the soil Machine release and organic acid make the highly testable land neutralized to release the compound in a variable and usable form to store ammonia (Ammonia) and other useful ships of the nitriding county. It takes a long time to form naturally: hot rot ^ ^ increase water binding capacity, and cranes over Tian Qiao pre-quality or peat. It can be several times, usually G3 to Μ U bin 8 ϊΐΐ or more. The resulting humus has a porous layer of woody cellulose, cellulose and hemispherical cellulose and between, or between 5% and 2%, its degradation rate, ice, oxygen, acidity and environment Biological activity and its regulation 3 related: The ρ Η value of the humus according to the present invention is post-treated to 5 to 6 or 6 to 7. The post-treatment of the humic acid f can be carried out by washing the ΡΗ value ^ ° before, during or after the storage of the reagents such as sodium hydroxide. The combination of the wheel 4 and the added ash 4 is basically the reaction product of the method of the present invention. The above characteristics are effective for the combustion characteristics of 68 201118162. By optimizing the processing procedure, certain materials in the humus can be concentrated, particularly by the difference in concentration between the solid and liquid phases in the reaction mixture. This is ideal when humus is used as carbon dioxide ((^( 库 / sink sink sink sink 或是 或是 或是 或是 或是 或是 或是 或是 或是 或是 或是 或是 或是 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 Concentration is undesired. In addition, 'avoid a large amount of inorganic and alkaline substances and other substances that are harmful to the use of the product. According to the case, the humus produced is a uniform humification and fuel' characteristics can be calculated 'Can be controlled by the composition of the feedstock and the catalyst and processing procedures. The humus produced according to this case can be produced in a few hours. Therefore, the method according to the present method is faster than other known methods of manufacturing humus, which usually requires a number of Weeks or months. 5 According to the method of the present case, the materials and/or fuels produced include peat _: or coal or similar peat or similar coal materials, which have the following characteristics: The biological f towel gets the charcoal (secret) to the coal-like fUel. • The fuel value is related to the ji procedure. The reaction time increases with the residence time in the reactor. The volatility is lower than that of conventional or fossil fuels with a ratio of carbon to 石化.7 to 〇.95. The lower the temperature, 90竓 to 95%: lignin or bacterial biomass. • The target is a petrochemical fuel with a total carbon phase of the phase, which is more/tongue and has a lower Auto-ignition temperature: • ar, or coal; δ fuel has a similar value to the fuel produced by the case, but its composition and miscellaneous “69 201118162 material is significantly different. Different types and types of fossil fuel It has very different chemical composition and characteristics, and is related to the mining area and the point of origin, so that each type of coal has unique and clear characteristics. For example, the petrochemical Lausitz raw material lignite has a fuel value of 8,700 kJ/kg and the water content is about 56. %, sulfur content is about 0.7%, and ash is about 4.5%. According to the case, the water content, sulfur content and ash content of the material or fuel are lower' and the fuel value is usually clearly higher than 2〇, 〇〇〇kj/kg 1 kilowatt (kilowatt) petrochemical L The ausitz raw lignite can be produced independently of the water content. In contrast, according to the case, the same amount can then produce more than & the amount of σ compared to fossil fuels, according to the material and / or fuel in this case The concentration of the Maynard reaction product can be detected. Νε_ (NKcarboxymethyl) lysine (CML) itself can be used as indicator 1 in the liquid phase of the reaction product and can also be detected in the solid phase. To this compound, a concentration of 0.2 to 1.5 mmol/mol or more of the lysine is measured, whereby a higher fraction can be measured in the liquid phase than the solid phase. The concentration distribution is related to the feedstock, reaction conditions and processing procedures. ° After mining, depending on the depth of the mining, fossil fuels are in the form of massive or relatively rigidly compressed agglomerates that must be ground with high energy. More progress must be dried and milled to fine-grained lignite or pulverized coal by a coal mill. In contrast, the material and/or fuel exhibits particles having a particle size of 1 mm to 30 nm after the end of the process, and because of its large surface, the grain is easily dried. Thereby, the dryness for adjusting the applied energy and especially the fuel is quite low compared to solid fossil fuels. .....' The characteristics of this fuel are particularly advantageous compared to the type of fossil fuel used in coal and the fuel that is currently available in recyclable materials. At least one of the following numbers, but usually several or all are more suitable for burning crude temple feed materials or other fossil fuels or biomass,,, 枓·reduced ash, less Gas, nitrate, sulfur heavy metals and lower 201118162 powder, fine dust and gas toxic (4) emissions, the quality of the noodle fuel and combustion characteristics of the feed material or feed raw paste, and the tender composition, And the feed material with the right amount of energy and the energy content allows the fuel to reach the process of turning over the sludge, and the calorific value is compared with the feed material having a fuel value of 17-20 MJ/kg, and After the dereliction of g _4 breaks the summary, its gray money is less than the value of 17-20 leg g of feed material, after burning tg dip, the sulfur content is reduced to gas ^ in the feed material, with Low fine particulate matter and lower combustion procedure steps, adjustment of associated fuel quality, and lean petrochemical fuel are products that are relatively pure and nearly ultrapure. The favorable characteristics of material reduction and stationability are mainly attributed to inorganic matter, which is also understood as 'God V. Phase is understood to be the combustible part of coal, and the purest coal percentage is disgusting. The inorganic content of the coal is, for example, less than the weight of ο.1. 71 201118162 The method of the last method is to burn the particles and the powder produced by the reaction product quickly and have a good cross section with a depth of about 1 to 2 cm and The angle of inclination "between the caps" can be ignited by the air in the combustion chamber. Si - the area of the larger mosquitoes makes the coal pens better. According to the case, the powder is impregnated on cellulose or The most suitable proportion of the ingredients is the contact and the machine side., the life + i f5 calorific value is 25 MJ/kg to 30 MJ/kg of powder or fuel particles 2, 7, (dllpped wood) or wood chips (w〇 The ratio of 〇d chip) is 53 : H % : 42 or preferably 64 : 36. Therefore, the amount of 3 water for cutting wood or wood chips is about H)%. The particles are not more than 2 coffees and less than 1.5 mm. Small can be less than 1 melon. • The calorific value is 22MJ/kg to 25 MJ/kg or the ratio of fuel particles to straw is 61:39, or it can be shame: or 72: 28. Therefore, the water content of the cut wood or the wood chip is about 1%. The particles are not more than 2mm, or less than h5mm or especially less than lmn^. Relative to the above ratio, powders containing peat or peat containing equal amounts of cellulose and lignin are processed into briquettes. Peat or peat can also be equivalent to cellulose and lignin alone. The processing becomes a briquettes. • The powder produced according to the method of this case and other materials containing cellulose and lignin or peat or peat are mixed together or mixed separately, 'for example, Conidur with a screen of 2 mm The impact filter is carried out in an impact tab mill. • The pressure is set at 100 MPa, which can be higher than 12 〇Mpa and also 72 201118162 can be higher than 140 MPa. • Press operation It is carried out at temperatures close to (6) and should not exceed 90 ° C. Its size is 250 X 60 X 50 mm. • The bulk density of briquettes is about 0.95 g/m3. to 1.15 g/ mJ ° Pellets produced from the reaction product according to the method of the present invention: The pellets produced by the method described in the present invention are preferably dried in a pellet after wet pelleting. This method is suitable for applying relatively low energy Pellets are produced from fuels with different heating values. • Good combustion allows standard automated combustion systems to be achieved in pellets. • For small combustion stations, defined emission standards can be met. The appearance of the fuel is in a small form and as uniform as possible. • The diameter of the pellets is from 3 mm to 7 mm, preferably from 4 mm to 6 mm. Its length is between 5 cm and 45 cm. The pellets have a high impedance or hardness, which produces only a very small amount of dust during the treatment process, and has high water repellency and can be properly dispensed. • Continuously feed the pellets into a fully automatic pill oven or vessel and burn in a controlled manner. • High heat performance with minimal inorganic pollutants or fuel gas emissions by burning as completely as possible. • When the calorific value is higher than 25MJ/kg and can also be higher than 27MJ/kg, use bonding material and combustion accelerator, especially wallpaper (waiipaperpaste), turf, straw 73 201118162 and Other lignocellulosic biomass. Or wood, such as the wallpaper f-aged organism f, can reach about 12-14% by example h n or the water content of wood chips or other lignocellulosic biomass. , the cellulose and lignin content in the ratio of the above-mentioned ratio 'peat powder or fuel granules', etc. are reinforced into pellets, so that the granules are not more than 2 sag, or less than 1.5 mm, and may be less than 1 mm. • Peat or humus as described in the method of the present invention can be processed into pellets separately with equal amounts of cellulose and lignin. Powder and cellulose-containing and woody gamma-containing materials or peat or peat concentrates The mixing is in the city, for example in an impact tab mill with a 2 mm Conidur release filter. • The pressure of the pressure is 1 〇〇. MPa, can also be higher than 12〇Mpa and rlj at 140 MPa. • The pressure temperature is close to 8〇t: and should not exceed 90〇C. • The most important adjustment for the pellet, especially compared to The pellets of fossil fuels are derived from improved combustion characteristics and in the field of sinter behavior of coal ash, ash treatment (usually lower ash) and the size of the combustion disc. 74 201118162 Energy can be thoroughly According to the method of this case, the ugly = there is Produced in the preferred embodiment. The fuel produced according to the ride is related to the adjustment performed in different devices. The pill _ type is usually a stove, a pill or an extension. _ Burning 111 is carried out and has automatic transfer supply. Combustion equipment with commercial seals can usually be used. In order to increase the characteristics of 峨, in the field of ϋ = 'The combustion equipment according to this case can be adjusted to the change of combustion · According to ash Adjust the form and size of the combustion disc. The smaller the ash, the smaller the diameter of the combustion disc can be used to produce better combustion. " • It is recommended to use an automatic device for removing ash from the combustion disc to prevent agglomeration of the combustion disc. The size of the naturally occurring pellets of this agglomerate, especially lignite. '"'pay* The combustion of the powder or fuel according to the present case is in a coal-fired power plant with at least one steam turbine. get on. In order to achieve high efficiency, the furnace is operated at a temperature higher than ·C, especially higher than 65 (). Further, by increasing the performance in high temperature regions by, for example, modern power plant technology, it is possible to achieve a sufficiently efficient combined gas turbine technology. The efficiency of current generation can be higher than 43%, or higher than 46% or higher than 49% to 55%. ' Coal gasification combined cycle power generation technology (IGCC) with integrated coal-carbon gasification is used for the combustion of fuel produced according to the method of the present case, i fluidized bed combustion technology can also be 'specifically with cyclic pressure A combined procedure for fluidized bed recirculation and power generation (PFBC) and, in particular, a combined power plant with coal-fired combined cycle power, such as pressurized pulverized coal combustion (PPCC). • The combustion program contains a gas entry temperature greater than 1 〇〇〇〇 c, or greater than 1200 ° C and may also be greater than 1400. 〇75 201118162 . The temperature gas cleaning method is designed in such a way that the particle content and the content of the active substance, especially the sodium and potassium compounds, and the corrosive gas are reduced to such an extent that the fuel gas can be immediately sent. The gas turbine 's preferably utilizes the low temperature plasma characteristics of the fuel gas. • The percentage of the volume of the particles having a particle content of less than 3 mg/m3 i n and a diameter d of less than 3 μm and a content of less than 0.01 mg/m3 i.n. can be achieved by a separator for separating the liquid slag in the fuel gas. β. According to the method described in the present invention, the method of generating a current or energy from a fuel (particularly a powder) is a use of a carbon fuel cell. By means of a shared energy generating device, in particular a turbine, preferably a steam turbine or a gas turbine for energy generation can be produced by and/or its seam inspection. _ Stomach. • Among these renewable energy sources, the Disputable Wind Power System (DWPS), in which the turbine is shared, especially the steam turbine or the gas coffee wheel, is (4). The compressed air is depressurized in a plenum chamber. The compressed air is then additionally inside the turbine that is already in operation. • If compressed air is introduced into a running turbine, its efficiency increases by 20% to 200〇/〇 or 4〇% to 170%, and may also be 6〇% to 15〇%. The efficiency is increased by introducing compressed air into the already operating turbine, and the efficiency lUT exceeds 2% to 2% or 4% to 17%, and may also be 6% to, according to this book. The device described in the embodiment, the different programs are combined in units. Grinding and mixing can be carried out in a single obstacle or in a space where the turbulence is impeded. In this (10), the device or the setting system of the injury system has a record. The possibility of the method or procedure step on the f 76 201118162. All the steps described above are equally feasible. Volume into (four) transfer money reactor batch

〇eil彡, Yatian sent the feed to the mixing vessel (6). By

The gluten-rich 0-wide culture vessel (8) allows the catalyst to remain on the material for a period of time. The contents If (7) and (8) are double-walled and have a hot water connection _ water connectlon so that the material can be preheated to 50 ° C to 60 ° C. The culture material of the feed material of the "dry" is fed through the conveying device (9) and (1〇) 3 'the tree of the tree is the se_ eonveyor or the conveyor belt, at a high The reaction ribs are fed from the first-feed strands via the inlet (21) under the pressure of the steam of the process water. The feeding device (9) is composed of a force conveyor, such as a syringe (injeCt〇r), a double screw extruder, an eccentric ?piml pump, a piston Pump _〇n pump) and spiral displacement pump, which may or may not be equipped with a spiral compressor or a double spiml compressor. The feeding device (21) can additionally be provided with a closing device 77 201118162 (shutoff device). The feed device (21) ensures that the strand I having a pressure level higher than the internal pressure of the reactor enters the reactor (19) and prevents backflushing (ba feed means.) Back eight has a relative volume of 3 The solid content of the feedable feedstock from % to 5% by weight is mixed with the process water (4) and the catalyst (15) in a mixing vessel (1 Torr) and passed through a suitable conveying device (1 Ό feed) In the reactor, the conveying device can be designed, for example, as a piston (9), such as a spiral displacement pump (spi), or an eccentric spiral pump. The material is heated via the heat exchange unit (18) to at least Temperature C to 220 C or 220 C to 250. (: In this way, the feed stock pretreated by the feed stock! is fed in parallel or afterwards via the feed material previously fed to or present in the conveyor. Guided by the feed strand, the ratio of the mass flow rate of the feed strand 1 to the mass flow rate of the feed strand II or the ratio of the existing feed to the feed is, for example, 1:20, 1:5, 1: 1 or ι〇: ι. Uniform mixing of existing or fed materials via a mixing or agitation device (20) at first The occurrence of heating and exothermic reaction with the reaction takes place via a heat exchange device (22) which is connected to the double wall (23) of the reverse g and/or via other heat exchanges The heat exchangers are provided in the reactor or connected to the reaction mixture. These heat exchangers can be, for example, spiral, tubular, bundle or ^-rotating Spiral heat exchangers. After the required residence time, the contents of the reactor are transferred to the second reactor (24) using a pressure drop. The means for accelerating the fluid can be used in conjunction with the flow. The pressure vessel in the direction behind the first reactor has a smaller volume because the process water is retracted using the apparatus described in another part of this specification, whereby the volume of the reaction mixture can be reduced. Further processes require less reactor volume or smaller reaction space. The recovery of process water can also result in a smaller reaction volume for combining different parallel reactors or reaction mixtures. 'It is combined in a single reactor in a parallel manner or in a time-delayed manner. The reaction phase deviates by up to 5 〇. The total reaction time of /0 or the reaction time deviates to 50%. The volume is 5%, 1% or 2〇〇/0 lower than the total volume of all reactors in the reaction mixture it receives. • The reactor (24) can also be equipped with a heat exchanger (22), agitating device (20) and the double wall (23)' and maintain the temperature in the residence time at the level required for the reaction. The released reaction heat is released via the heat exchanger (22), thereby achieving cooling: in the reaction After the residence time of the device (24) is over, the material is liquefied in the liquefaction vessel (26) via the heat exchanger unit (25). This material can be heat treated via agitation means (20), heat exchanger (22) and double wall (23). The heat exchanger (27) ensures that the material cools to a temperature below the evaporation temperature of the water. Thereby, the fluid and pressure liquefaction are controlled via a reverse-directed liquefaction pump which can be formed by a force conveyor, a deviating screw pump, a screw displacement pump or a piston diaphragm pump. The wet feedstock is stored in a liquefaction vessel (29). The accumulated heat can be released via the double wall. The excess process water is separated by a subsequent solid-liquid separation device (3〇), and the solid-liquid separation device is designed as a decanter, a centrifuge, a cyclone, and a filter cavity press device ( The fllter chamber device, the filter device or the device for separation or drying, which has the same purpose or described elsewhere in this specification, is again available for use in other processes for the method according to the invention. The final product is temporarily stored in the reservoir (31) for further use. The feed to the first reactor or the several first reactors can also be carried out via a single feed strand, i.e., independently via the feed strand I or the feed strand or independently of the second feed strand. If it is feeding the "wet" feed material, ^ is no problem. However, when the reactor is filled with “dry” and free-flowing feedstock, it is necessary to consider that there is sufficient water supply. Process water or concentrated process water at temperatures above 6 (TC, 10 (TC, 16 (TC or 20 (TC or 20 is advantageous for use, where less than free flow or feed for "dry" feedstock) Filling up to 5%, 10/〇, 40% or 60% is sufficient. Filling the process water in the reactor 79 201118162 plus height and bulk density of the feedstock and other concentrates ( Consistency and so on. Vapor, according to the invention, in order to increase the output of the feedstock or the fuel or material, it is necessary to increase the content of the g] as much as possible. The limiting factor - the aspect is mainly wet biomass J, and the other is that the pump with the dry biomass connected to the reactor has no "sex". It should be considered that the dry biomass must also be pre-small enough. During the filling method, the viscosity = the degree of decrease is reduced to more than 3/4 of the viscosity of the feed material, or more than 1/2 or 1/5. However, the residual material of the strain and the active use of agricultural products And the importance of the environmental sanitation θ treatment is increased by the fact that it is located in the fermenting solution Upstream hydrolysis and especially the so-called disintegration of the bio-f of lignocellulose = lignocellulose, such as wood, grass and twigs and fuel manufacturing, while ί/ii gives economic and safety options such as animal wins The use of the law; the use of the law of the 'animal diet is difficult to produce, following the treatment of the green, the greening of the money, the use of biomass of money waste relative to the use of the phase method i, (fernter) before the 'pretreatment of biomass The thermal hydrolysis of various raw materials and raw materials has been developed a few years ago, and the original reactor is looped by a loop reactor (as disclosed in the public document 201118162 (4) or hydrolyzed (such as Public Documentary 28815). Said) Guided and heated to 18 〇t. Microbial hydrolysis system (such as the public document DE gamma 391_) towel. & type reactor to go to SI: gas equipment for the heat of the temperature in the boots 2: this period The two benefit-capacity's are actually unable to present a wide range of deficiencies that have been unsustainable and have been unable to sustain the desired solids. 2, Ό ^ f is emitted in a heat exchanger formed into a tubular exchange 11, II Some problems that last for many years can only By reducing the solids content to avoid 'and the H-like drop of the low-transfer donation of the feedstock yields the economy can be practically impossible. _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ —) Role and t-structure _ bulging side and the heat of the starch in the crop; Γ 尔 尔 underestimate. Expansion system - kind of solid body: reversible volume increase at the beginning of steaming. Watery and swell. _ and chemical _ bulging scale is Wei _. In the physical, such as water will be in the holes and voids of the wood chips. The surface tension in water and wood chips is called capillary force (c, and there is a chemical light procedure in which water is added to the hydrophilic knot f tt hydroxyl (0Hgn) up). In the plant structure, water is stored between the polysaccharides of the cell wall. During the expansion process, the gel _tine, the peak, and the colloidal structure (c〇u〇idai stmcture) will be temporarily produced. Decomposition - Some protein substances such as bones and skin waste are colloidal substances that can be expanded in water. Starch is produced in nature and appears in the form of fine powder of the temple powder, which can be i=L==°f/M_(suspend ° ° It is mainly between the temperature of 47c and 57C. In the higher temperature pit to the order between the fine particles will be trained. Amylase and Qian Lin (amylGpectine, into the temple powder Less, such as potato (four) on the starch secret point and small) wheat

Q 81 201118162 The wheat starch is 67.5. (: The viscosity of the solution is thus greatly increased, and the gel is formed. Traditionally, the gel can also be called a glue, and these gels act like colloids. The whole process of swelling and gel formation is called glue. Gelation. Starch colloids have different stiffening capacities, which are related to the type of starch. The swelling effect is increased again by pressure and heat, and accelerated under conditions of thermal hydrolysis. It can be known that Miyazaki varies greatly in different biomass towels. In corn silage, for example, it can be between 12 and M4 by weight relative to dry matter. The ability of corn silage is greater than that of wheat powder. Glue and larger than Ma Ling Wei Na ^ corn silage is a kind of biomass that often produces biomass. The hydrolysis process especially needs to consider its high hardening ability to avoid the blockage of the heat exchange system. Consider low starch content such as low 5% can improve pumpability under certain conditions, especially at fixed temperature to pressure ratios. However, with thermal hydrolysis, 'pressure and temperature are fast When increasing, the volume increases and therefore the flow resistance increases must be considered in advance. The feed has a high starch content, for example more than 10-30%, 30-50% or more than 5 相对 relative to the dry matter. It is the biomass system that is directly introduced into the first reactor via the strand (10) (four) for "dry" biomass, that is, the feed strand, and where the liquid from the strand is coated. Biomass, and/or mixed with it. It has a 3%, 5% or 10 / relative to the dry mass. The following low starch content biomass or feedstock is introduced via the feed strands, which may be fed with or without pretreatment. The increase in the formation of the product and the blockage may be due to a combination of various factors. The formation of the program gas in the heat exchanger and the expansion of the starch play a major role in increasing the volume. Ideally, it is assumed that the tubular reaction H towel has a plug away from the opper 〇W): this can be expected to increase in volume depending on the gas formation or expansion, and the force Jk increases. It is also additionally increased by the increased viscosity of the starch of the delivered product (g〇〇ds). Therefore, the fluid resistance will also increase. 82 201118162 “ ίί 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽 纽It is a method of adding, in particular, a higher yield relative to the solid content, which is used in the present invention for hydrolysis or for heating biomass, and is characterized in that it is heated by heat exchange ii and solidified. The liquid mixture is passed through the pair of pipe fittings in a flat gravity to avoid agglomeration and/or flow. The material itself moves downwards and does not need to be considered to be gravity. To prevent agglomeration and blockage In this embodiment, the heat exchanger device is at least 20 degrees, 40% or more. In the embodiment, the axial direction of the pipe member is relative to the horizontal plane 3. The degree of y is greater than or equal to 10 degrees. The heat exchanger is at least 20%, 40% or . Vertical f-pieces. Vertical pipe = attached to it, the angle is 7 degrees relative to the vertical plane, and the vertical angle is less than 45 degrees in the vertical direction. In the embodiment, the vertical pipe part _ Straight limbs up to 1 degree. ^ ΐίί f1 ^ such as f-type reverse wire or The reaction 11 is formed by a combination of a plate or a heat exchanger. The heat exchanger is modulo and can be composed of different modules, units or sections. The heat _ unit energy gamma 11 blending system consists of two layers, which are made up of thermal energy. The thermal energy carrier f can be, for example, hot oil, water vapor or a method of process or other process water. Combine different carriers; 1 quality. The target temperature of the medium (4) et temPerature) at 60 ° C and r + «HI. In the first section or the first mode _ temperature system such as 6G ° C to 100 i =? = i12G °C 'between the temperature of the second section or the second module, for example between 12 叱 and _ 'in the temperature of the third section 丨; between 40C and 180C or 16 〇. (: and 2 〇 (between TC, and in the fourth district 83 201118162 Yan Wenwen is between 18... and fine ^, 22 (Γ (: and "..

Between Cf3500. The temperature of the heat carrier medium can vary by up to 2 °c, 4〇〇c or = °C. The units, modules or sections of the heat exchange H are connected in series such that the temperature of the solid-liquid can be lowered to the inlet or outlet temperature after reaching a maximum temperature of, for example, 22 〇〇 c to 26 。. Corresponding to the zone sanitation-hydrolysis reactor, it is possible to maintain the material at a positive or negative 2C to 8C level and to ensure a residence time of, for example, at least % minutes. There are dual-purpose smashing devices. This is used for solids containing a certain amount of age, such as m (10). Here, the "dry" creature has been in the Yuzu 1 plate discharge container (2). The feed material is fed to the rotary conveyor or a conveyor belt via a conveyor and is controlled by =. The mixture is transferred from the reservoir (4) and the second reactor. The catalyst is completely mixed on the material. (8) There is a hot water connection to preheat the material to 50. (: to 60. (;:: ~ /, "dry" feed material of the feed material is fed into the reactor feed device (9). The feed device contains, (stoppmg apparatus). The feed device makes The pressure of the cultured material f-reactor is fed to the reactor (19) and prevents the chargeable pump from having a solid content of 3% to 8% relative to the overall volume. 201118162 The feed material is fed through the feed. The strand II is mixed with the process water (4) and the catalyst (15) in a mixing vessel (14), incubated (16), and fed into the reactor via a suitable conveying device (17) (the conveying device (17), for example Piston, helical displacement, or offset helical pump.) The material is heated via a heat exchange unit (18) to at least i8 〇 ° c to 200 ° C. In the hydrolysis reactor (21), from the feed π The fluid, pumpable biomass is mixed with the dry biomass from the feed stock. The material can be additionally thermally affected via the heat exchanger (22) and the double wall (2〇). After the residence time has elapsed, the liquefaction of the material enters the liquefaction vessel (25) via the heat exchange unit (23). The heat exchanger (23) reads The material is cooled to a temperature below the evaporation temperature of the water. Therefore, the channel and pressure liquefaction are controlled by a backward-oriented devolatilization pump designed as a force transfer device, an off-axis spiral, a helical displacement, or It is a membrane type fruit. * A wet feed material is stored in the liquefaction vessel (25). The accumulated heat can be released through the double wall. The excess process water is separated by the subsequent solid-liquid separation device (4). The solid-liquid separation device is designed as a glass bottle ((1), centrifuge, cyclone, filter cavity press device er, such as P_ng device), filter device or for similar purposes or The apparatus described in the section is described herein, and the process water may be further provided for other procedures in the present invention. The final product is temporarily stored in the reservoir (27) for further use. Widely operated in a continuous manner, that is, the feedstock is sent to the processing time via a reaction to a heat exchange of the material for a desired period of time, a phase of six __ for the addition to the heat exchange sequence, Or in points The branch (.running) method is added to the liquefaction vessel (m to ° so the yield of the equipment is received by the transport I (17) and the induction device is received = 丨. The reverse directional liquefaction 1 (24) rotation speed is different in the device The liquid can be evaporated with the pressure existing in the equipment. 85 201118162 The liquefaction device or the liquefied fruit can be controlled by temperature and / or Lili, and the reduction can be obtained when the hot money II towel is longer. The temperature of the medium is thus lowered. The temperature is adjusted according to the J required in the subsequent device or in the subsequent step, for example, if the reaction mixture is further introduced into the container having the ambient pressure, the temperature must be adjusted to be lower than the axis. Qing is exempt from the controlled evaporation process. According to the embodiment described in the other part of the description #, feeding to another dry county order 'will require a temperature higher than the miscellaneous temperature 0 to control the residual pressure of the liquefied pump 2 enough to use 5, 2 The delivery of the latter procedure or device towel. The remaining thief _ force is, for example, less than 10, r. Or 1 bar. ... The design of the stock for the touch _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ All the equipment connected to the double-feed raw materials are as much as possible in terms of technology and kiosk, system, adjustment and automation. This is also valid for all mentioned procedures, methods or sequence steps. ~ In the process of the method, the decrease in _ degree can be observed as a measure of water sputum. The viscosity of the solid-liquid mixture is reduced by the hydrolysis of the solid-liquid mixture by at least 3/4, 1/2 or 1/5 of the feed material. It must be adjusted as high as possible to increase the yield of the feedstock or increase the yield of the feed. The limiting factor for maximizing the solids content - in terms of the nature of the delivery, and the connection to the pilot reactor independent of the pump, the transportability of the micro-dry biomass. According to the method of claims 37 and 38 of the invention, the production of the ceramic material produces a suspension dispersion. , the manufacturing method of ^, the object is the root shot, the patent scope is taken. The void of the carbonaceous material before the at least part has a structure including ceramic and carbonaceous materials or other substances. The manufacture of all or part of the ceramic material, such as the assembly or the consumption of 86 201118162 ^^^^ eve (10) surface - (four) ' is very complicated at present, T is very high intensity f, difficult to shape or Mechanical processing after 1 。. Nucleation is a non-toxic high-temperature ceramic, especially because of its excellent properties, such as hardness, optical transparence, semiconductor properties, high thermal conductivity, and resistance to text. 'Therefore it is used in many different engineering fields, such as the manufacture of refractoiy materials, insulators and as semiconductor materials. The manufacture of tantalum carbide articles is of high economic importance. The material of the conductive material 1,4-carbene is usually formed by a conventional sintering method in which finely ground cerium carbide powder is baked at a high temperature by using a different bonding agent. A disadvantage of this procedure is that in addition to the high temperatures and long sintering times required, the resulting articles are porous so that they can only be used in certain applications. Another method for producing a carbonaceous material, the method of producing a carbonaceous material, such as graphite, is known in the publication DE3322060, which is accurate in measurement and shape, and then, in an anneaiing treatment for a long period of time. Substituting the carbon of the object at least close to the surface by yttrium processing, squeezing the material into a granulated material of the oxidized stone during annealing, and guiding the hydrogen gas, for example, during annealing Through the granular material. Thereby, a gas having an interesting yttrium oxide which can diffuse into the carbonaceous material adjacent to the surface of the object and react with the carbon of the object such that the lanthanum carbide is formed in the matrix of the object can be produced. Thereby, the exchange of carbon and niobium carbide of the object can be accomplished at least adjacent the surface, thereby achieving a considerable improvement in the area of the adjacent surface of the object. A disadvantage of using this procedural method is that the production of cerium oxide gas is complicated, and it is difficult to maintain and ration the amount of cerium oxide required in this gas. The object of the present invention is therefore to provide an improved manufacturing method for a Tauman material, in particular carbonization; an object in which a carbonaceous material or a porous ceramic material, in particular a tantalum carbide, can be used in a simple and safe manner. Completely or partially converted to tantalum carbide. By adding a solid-liquid mixture of water and carbon as a starting or additional substance for generating a heat insulating material and/or a ceramic material, an incidental substance 87 201118162 suspension or dispersion can be obtained, and the composition thereof The temperature exceeds the excitation. c and pressure f ^ bar for processing. It may be excluded by the high purity of (iv) floating liquid (suspensiGn). Sulfur and ash are added as additives (IV) float or dispersion, the purity of the characteristics, other parameters, such as metal, chlorine, carbon, office, town, chromium, copper,! S, zinc is also the same. By increasing the amount of purified water or process water = plus the content of the above substances is correspondingly low in the carbon-containing solid-liquid mixture. The higher efficiency is developed by the side-sanding step to increase the carbon pressure in the solid-liquid age. Thereby, the contribution/disambiguation of the Wei compound is reduced to y 50 Α or 75/ί> with respect to the content of the carbon component. Sulfur and ash can be reduced by more than 80%, 90% or 99% relative to the individual raw content of the carbonaceous component. Or it is called Weisha, in the process of cleaning with the _ anti-hybrid, the sulfur and ash continuously decrease, and when it approaches the end of the program, it is reduced to more than 2/1〇 of the sulfur and ash of the feed material. The 1/12 or ι/loo mash is acidic because the pre-culture and addition of the (4) catalyst in the acidic medium provides an assay solution that provides the material itself. Use sol·Jingxian to add miscellaneous (4) secret liquid or fraction to the alkaline sol in the thief _ order _. The hybrid and the sol containing the rich or inorganic Wei salt and/or cerium oxide are produced via this treatment method and further method steps. Turn into an aqueous solution of water. The carbon-based salt component is used to make gels. The 郷 domain to carbon cut (4) produces a porous slag type provided by carbon gas permeation. Lai Wei contains purified carbon, pure carbon and high purity carbon. It is particularly important that the carbon is finely divided into high-carbonized cerium-like materials. When the granular material is heated, the cerium oxide reacts with the carbon immediately, thereby forming a carbon-containing fossil (the gas 'is preferably mainly pure Carbonized Wet body. The distribution of carbon in the day of the dioxide can be achieved by the small size of the carbon particles in the additional substance suspension or dispersion, whereby the formation of the cerium-containing cerium gas is substantially lower than that of the carbonized stone. At sublimation temperature, especially the temperature is already between 1700 ° C and 1900 t. 88 201118162 This, in a more advanced way, directly spreads to the object. By borrowing from m · char ί, the object comes from The carbon matrix (4) (10) is punctured in the heart dn. By this, the main enthalpy of the matrix of carbon in the carbonized smash is replaced by the structure of the main component of the base f, and the characteristics of the object have been angered and improved in the manner described. And the object's shape program produces a rich shot (4) 〇 n Gu Chu (four) granules = order to produce carbon-rich cerium oxide granular material, can be very ▲ and 2 to immediately react with carbon and other substances that want to add people Immediately available for access to surface surfaces The method for producing an object is known from the publication DE 10 2006 055 469, wherein the object is produced from at least part of the vacancy of the carbonaceous material of the carbonaceous material, wherein the final (four) and/or green The size of the object in the first step is to form a carbonaceous material, and then the object of the carbonaceous material is at least partially surrounded by the carbon-rich ceria particulate material, and at the annealing temperature, at least - annealed , where dioxobic = vine = release sulphide-containing gas, which penetrates the object and converts some or all of the carbon-containing material into a carbonization dream. If the sol-gel procedure utilizes soluble hydrolyzable inorganic or organic citric acid It is advantageous to use a salt as a starting material to produce a carbon-rich ceria particulate material. A variety of viable starting materials are included therein, which are suitable as a ruthenium supply, and can be applied to a sol. In the gel procedure, the substances explicitly mentioned below are only the particularly preferred ones of the previously classified substances and cannot be regarded as a summary list of the substances to be used. Glass 89 201118162 Glass can be used as the starting material for the sol-gel procedure using inorganic citrate. This continuation method is characterized by the scope of patent applications Nos. 36, 5, 72, 98, 103, 115 and 143 and Its subsidiary item. The specification for further continuation of the continuation method can be derived from the properties contained herein, wherein the carbonaceous feedstock feedstock is supplied to the first reactor, and the reaction mixture is passed in a batch manner. Guided to the next reactor, and the reaction product is continuously released from the final counter. The above-mentioned towel is more patented and includes the features and equipment of the device and device for performing the connection method. Characteristic combination. [Simplified description of the drawing] Fig. 1 is a schematic longitudinal sectional view of the reactor according to the present invention, and other components of the apparatus according to the present invention; Fig. 2 shows a cross section of the reactor wall area according to Fig. 1; Fig. 3 is a schematic view showing the apparatus in an exemplary manner; [Explanation of main components] 1 Hopper 2 Floor discharge container 3 Grinding device 4 Reservoir (process water) 5 Catalyst 6 Mixing container 7 Feeding device 8 feeding the culture vessel 9 feeding apparatus 10 further device 14 of the mixing container 15 a schematic view of FIG. 4 shows the catalyst; and still another schematic view of the display apparatus 5. 201118162 17 Conveying device 18 Heat exchange unit 19 Reactor, induction device 20 Mixing or agitating device 21 Feeding device 22 Heat exchange device 23 Double wall, heat exchange unit 24 Second reactor 25 Heat exchange unit, liquefaction container 26 Liquefaction container , solid-liquid separation device 27 heat exchanger, reservoir 29 liquefaction vessel 30 solid-liquid separation device 31 reservoir 91

Claims (1)

201118162 VII. Patent application scope: 1.  A method for producing and treating a material or fuel, humus, Maynard or the like from a solid-liquid mixture of water and a carbonaceous component, wherein the solid-liquid mixed character is at a temperature exceeding 100 ° C and At a pressure of more than 5 bar (bar), the starting material is continuously fed into a first reactor via a heat exchanger at a reaction time of at least six tenths, and the reaction mixture is in batch mode. The reactor is passed to the next reactor, and the reaction product is continuously released from a final reaction at a reaction time of at least six tenths. 2.  The method of claim 1, wherein one batch is at least 10 to 25 mass percent of the individual helium reactor or at least 25 mass percent &amp; ratio reactor capacity.  The method of claim 1 or 2, wherein the batch used to avoid backmixing is retained in a closed reactor for at least one percent of the reaction time 'the closed reactor is flowing The direction is set at least in the first reactor. 4.  The method of claim 3, comprising closing the control reactor via a closed component such as a pressure valve or a shut-off valve. j 5.  The method of any one of the preceding claims, wherein the capacity of the batch is not more than 6%, and the capacity of the batch is fed to the closed reactor. 6.  A method according to any one of claims 1 to 5, wherein the plurality of batches having residual reaction times of similar length are combined from at least two reactors into the next reactor. &quot; 7.  The method of claim 6, wherein the residual of the combined batch is reversed. Time ## Deviation from the longest residual reaction time of the batch being merged  Such as the scope of application for patents! The method of claim 7, wherein the last reactor is another heat exchanger. 9.  The method of claim 11, wherein the heat exchanger can be a tubular reactor with a blending system, a double tube heat exchanger, a tubular bundle, or the method of any one of the claims. A heat exchanger or a plate heat exchanger or a combination of the above. 10.  The method of any one of clauses 1 to 9, wherein the heat exchanger for heating the starting material flows through the starting material at a reaction time of at least six tenths. 11.  The method of claim 8, wherein the other heat exchange means for cooling the reaction mixture flows through the starting material at a reaction time of at least six tenths. The method of any one of clauses 1 to 11, wherein the reaction mixture is guided through the reaction mixture as it is directed from one reactor to the next. - heat exchangers. 13. The method of any one of clauses 1 to 12, wherein the reaction mixture is directed through a heat exchanger for decompression (decompressio, as described in the scope of the patent application, wherein The heat exchanger is separated from the reaction mixture by at least two-sixth of the reaction. The method of any one of the preceding claims, wherein the heat exchange (10) is constituted by a number of side analogous units and/or has a model structure. </ RTI> </ RTI> <RTIgt; </ RTI> <RTIgt; </ RTI> <RTIgt; </ RTI> <RTIgt;  The method of the tubular reactor of the present invention, wherein the method of the tubular reactor of the method of claim 18, wherein the double of the tubular reactor is The middle space of the layer wall. ", war" enamel machine 20 · The method described in claim 19, hot oil, steam or process water (p ss water). ~, 'this carrier The enamel is 21. For example, the scope of the patent application, item 19 or item 2, of the thermal energy carrier medium is combined. The method of rose, which is different 93 201118162 22. The method of any one of clauses 19 to 21, wherein the final temperature of the thermal energy carrier medium flowing through the heat exchanger is between 6 and 350 °C. twenty three.  The method of any one of clauses 15 to 22, wherein the heat exchanger is composed of different modules, units or sections. twenty four.  The method of claim 23, wherein the temperature of the first block or the first module of the heat exchanger is 仞 it to 1〇〇°c or (8): to 12〇, In the second. The temperature of the segment or the second module is between 丨(9) force and 14〇〇c or 120. (: and 16 (between TC, the temperature in the third section is between 14 (rc and 丨 (10). It is between 160 ° C and 200. (: between, and the temperature in the fourth section丨 它 它 it and 220 ° C, 20 (TC and 24 (TC between or between 240 〇 C and 350. (: between. 25.  . The method of claim 22, wherein the heat transfer device is the same. The units, modules or sections are connected in series such that the temperature of the solid-liquid mixture is a lower inlet or outlet temperature after reaching, for example, 2〇 to 26 (the high temperature or peak temperature of the TC.) The method of any one of claims 1 to 25, wherein the heat exchanger is provided with a holding passage so that the temperature can be maintained from 1 C to 8. The uniform level of the crucible. . A method according to any one of the preceding claims, wherein, after the anti-ship compound is passed through a heat exchange crucible, the anti-flight compound is introduced into a stir or The reactor of the mixing system, or a reactor at least twice the height to mix or disperse. The method of any one of claims 1 to 27, wherein the components consist of a starting material and a water-clearing agent. t. The method of claiming one of the scopes of the patent scopes 1 to 28, the batch of the chest coffee system is shouting, anti-knocking, process water or i as described in the scope of the patent application. The method wherein the component, the reaction product, the process water or the catalyst are at least at a percent of time. The method of claim 29 or claim 30, wherein the reaction product, process water or catalyst is added during a residence time of the reactor during a residence time of at least one percent during a residence time of the batch of 94 201118162. 32.  The method of claim 31, wherein the added process water is processed. 33.  The method of claim 32, wherein the processing of the added process water comprises at least one solid-liquid separation or other water conditioning. 34.  The method of any one of clauses 1 to 33, wherein the method is carried out under exclusion of oxygen. 35.  The method of any one of claims 1 to 34, wherein the treatment of the solid-liquid mixture consisting of water and a carbonaceous component is hydrolysis. 36.  - a pumpable secret liquid or a granulated substance prepared according to one of the scopes of the application of the scope of the application of the third to the 35th, wherein the temperature of the towel exceeds 10 ° C and A solid-liquid mixture of treated water and a carbonaceous component at a pressure of more than 5 bar produces the pumpable fuel suspension or dispersion characterized by: a mountain comprising at least 4% solids in the suspension or the dispersion Amount and at least carbon content. 37 An additional float or dispersion made according to one of the methods of claim 5 to 35, wherein the temperature exceeds 1 Torr and the pressure exceeds 5 bar Under the condition of treating water and carbonaceous components, the solids or dispersions and the liquid or dispersion are used to manufacture materials, characterized in that: VIII, the suspension or the dispersion comprises At least 4% by weight of solids and at least 5% by weight of carbon!! Two methods of using a mixture of water and a carbonaceous component as a starting material or a substance to produce a heat insulating material and/or a ceramic material, wherein Treating the solid-liquid mixture under the condition that the temperature exceeds 00 C and the Lili exceeds 5 bar, which is characterized by the fine content of the reduced portion, and the solid-liquid mixed sulfur and/or ash portion is applied for the third day. In the method described, the cap mixture is acidic and the ceramic material is produced by an alkaline sol (sol). Θ文注 95 201118162 40.  For example, in the method described in claim 37, the sol-gel method is used to sneak a fine smear, and the acid suspension (four) is initially recorded. Add to the glue  The method according to claim 39 or 4, wherein the sol comprises the inorganic salt (Silieate), the second meal, the sage, and the water glass, as claimed in claim 41. Or the method according to item 42 is a gel of a carbon compound and a phthalate compound. Ϋ3 === The 43rd 檐 檐 檐 檐 檐 檐 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第 第Porosity model. 47.  The method of claim 46, wherein the smear type comprises graphite. 48.  Such as the scope of patent application! The method according to any one of item 47, wherein the material produced is tantalum carbide, in particular, tantalum carbide or tantalum carbide (SiSicj. = · a type of equipment; The liquid mixture is a solid-liquid mixture of water and a carbonaceous component, the apparatus treating the solid-liquid mixture at a temperature exceeding 1 〇〇〇c and a pressure exceeding 5 bar, the apparatus comprising a reactor characterized in that : The inlet device comprises a pump for conveying a solid-liquid mixture having a solid content of at least 10 mass % or to 15 mass percent, or a heat exchanger wherein the tube axis is at an angle greater than 1 degree to the horizontal plane ' ' A device for treating a solid-liquid mixture, which is a solid-liquid mixture of water and a component, which is treated at a temperature of more than 1 Torr (at a temperature of rc and a pressure of more than 5 bar) a solid-liquid mixture comprising a reactor, characterized in that: a hydrolysis device comprising a pump for delivering a solid-liquid mixture having a solid content of at least 〇 mass percent or at least 15 mass percent, or a heat Switch, 9 6 201118162 The angle of the tube axis to the horizontal plane is greater than 10 degrees.  For example, the device described in claim 49 or 50, wherein the fruit is an eccentric spiral pump or a piston pump (piston pui^: 52.  The apparatus of claim 51, wherein the pump is designed to have a pressure of 1 〇 130 bar. 53.  The apparatus of any one of clauses 49 to 52, wherein the heat exchanger is composed of at least 60% of vertical tubes. 54. The apparatus of any one of clauses 49 to 53 wherein the hot parent exchanger is for conveying the solid-liquid having a solid content of 3% to 50% and consisting mainly of biomass. A mixture of lignocellulose and/or starch-containing material. + * μ. For example, the hot parent converter is designed to be used for a temperature of 603⁄4 to 3 °C, or to a group, or a group, as described in one of items 49 to 54 of the The unit is for 2〇〇. (: to a temperature of 3 ° ° C. 夕 56 · as claimed in one of the 49 to the first item of the patent scope, the hot parent converter is designed for 10 bar to 丨 2 〇 The pressure, or module, or a unit is used for a pressure of 60 to 12 bar. ^57. The heat exchanger according to item 49 to item 56 of the patent application scope or at least - The module or unit is designed to be used for up to 250 parts of item 57, to prevent "quality contact, the tube is * heat resistant and anti-rice and 59.   Contact device, wherein the heat exchanger and the medium are described, wherein the heat exchanger and medium are 97 201118162 6]. For example, in one of the 49th to 60th claims, the heat exchange H is a tubular reaction H with a blending system, a double bundle, a bundle bundle heat exchanger or a plate heat exchanger. Or the above, and the person °. 62. In one of the 49th to 61st applications of the patent application, the heat exchanger is composed of a plurality of similar units and/or has a modular structure. Mounting the device described in item 62 of the L3 ' ' ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ ─ The apparatus of any one of clauses 49 to 64, wherein the blending system of the tubular reactor is composed of a double wall. 66. A device as claimed in claim f65, which is noisy by the tubular reaction H.雠〃 系 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如 如Μ "Buy for 68. The device of claim 66 or 67 is designed for different thermal energy carrier media.夂,,, 69. As claimed in one of the items 66 to 68 of the patent application, the heat exchanger is for the final temperature of the thermal energy carrier medium (6) and 35 〇ΐ 70.  The device of any one of clauses 66 to 69, wherein the hot parent converter is composed of different modules, units or sections. 71.  The device of claim 5, wherein the hydrolysis device comprises a counterpressure pump (72.  a method for producing a fuel, a carbonaceous material or substance, a humus, a Maynard or a similar reaction product, comprising treating the water and the stone-containing anti-ingredient at a temperature of more than 1 ° C and a pressure of more than 5 bar A solid-liquid mixture, such as biomass, characterized in that the treatment is carried out continuously. ,,’ 73.  The method of claim 72, wherein the treatment lasts for at least one hour and/or includes adjustment of biomass processing and/or reaction products, intermediates, secondary products 98 201118162 and/or final products. . 74.  ^ The method described in Article 72 or Item 73 of the patent application, in which the adjustment is made. More than 16G ° C, preferably at 16 。. (Between and between classes, especially between 225 C and/or with automatic control.)  The pressure is adjusted to at least 7 bar, preferably between 1G and 34 bar, between 10 and 17 bar, 18 bar, in one of the items in the 72nd to 74th paragraphs of the patent application. 26 bar or 27 bar and 34 bar, such as the scope of application for patents 帛 π to 75, wherein the processing time is at least 2 hours 'the chick is 3 small 6 (M, hour, especially good hours to 30 hours or 3 divination, 6 (M, when 'yous 13 hours to 24 hours. J 77.  As described in one of the claims 72 to 76, the treatment product is selected according to the type of the organism f and/or the desired reaction product. 78.  The method of any one of claims 72 to 77, wherein in particular, paste water, grinding, pre-incubation with an additive, and heat mixing to pretreat the biomass. 4 疋 pre-, with acid 79. The method of claim 78, wherein the biomass is cultured at a pre-treatment pH. 80. The method of claim 79, wherein the pH is less than 6, preferably less than 5, more preferably less than 4, particularly preferably less than 3, and especially less than 2 °. _ , 81.  The method of any one of clauses 72 to 8, wherein the organism f is ground, preferably shredded or ground, before, during or after the treatment. ' 82.  The method of claim 81, wherein the milled biomass has a particle size of less than 10 cm', particularly preferably less than 丨 cm, especially less than 2 mm. Eight, 83.  The method of any one of clauses 72 to 82, wherein at least one catalyst is added to the biopterin before and/or during the treatment. 84.  The method of claim 83, wherein the catalyst consists of a plurality of non-99 201118162 identical injuries. The components together form a catalyst mixture. 85. The method of claim 83, wherein the catalyst is a mineral acid, preferably sulfuric acid, and/or a monomer, a binary or a ternary tannic acid, preferably tartaric acid. Or zen sour. 86.  The method of claim 85, wherein the acid is used as a catalyst and simultaneously used to adjust the acidic pH in the culturing step. 87.  The method of any one of claims 83 to 86, wherein the catalyst comprises one or more metals and/or metal compounds. 88.  The method of claim 87, wherein the metal and/or metal compound comprises at least one transition metal of the subgroups ia, na, iva, va, Via, and Vila in the periodic table, preferably Nickel, cobalt, iron, copper, chromium, tungsten, molybdenum and titanium, and especially iron. The method of any one of clauses 83 to 88, wherein the catalyst comprises at least one biocatalyst, preferably an enzyme, a micro organism, or a plant cell (vegetable) Cell), animal cells (animai cell) and / or cell extract (cell extract) 〇 90.  The method of any one of clauses 72 to 89, wherein the biomass is mixed prior to and/or during the treatment step, preferably by moving, mixing, suspending and/or stirring. 91.  The method of claim 90, wherein one or more mixing devices are used for mixing, in particular a combination of different mixing devices, preferably at least one fluid jet mixer, pump or A nozzle (nozzle). 92.  The method of any one of clauses 72 to 91, wherein after the treating step, the reaction product is dried by a dryer, preferably a pair of convection driers or contacts. A contact drier, particularly preferably a stream and/or a band drier and/or a fluidized bed drier. 93. The method of any one of clauses 72 to 92, wherein the process water produced during the process is preferably recovered via a solid-liquid separation device and/or cleaned and returned To the reaction mixture. The method of claim 93, wherein the solid-liquid separation device is at least one for micro filtration, ultra flirtation, nanofiltration. And a combination of reverse osmosis or a combination of the above various devices, in particular having a ceramic element and preferably a rotating disk and/or centrifugation Centrifugal membrane filter. 95.  The method of any one of claims 72 to 94, wherein the wastewater produced by mechanical, chemical and/or biological cleaning is cleaned. 96.  The method of any one of clauses 72 to 95, wherein the waste gas produced in the treatment, processing and/or adjustment is cleaned by mechanical, chemical, and/or biological means. 97.  The method of any one of clauses 72 to 96, wherein the reaction product, intermediate product, secondary product, and final product comprise a peat fuel from a brown coal to a brown coal Black coal-based fuel (black c〇aWike fUel), humus, Maynard or similar reaction product, carbonaceous material such as damping substance, nano sponge, nano pellet (Curry pellet) ), nano flber, nano cable (nan 〇, activated carbon MM coal) or sorption coal, charc〇al material, highly compressed carbon products and materials, especially Starting materials for graphite and graphite or near graphite products as well as carbon fibers and starting materials for composite or fiber compound materials. ... 98.  The method of any one of clauses 72 to 97, wherein the material or fuel, humus, Maynard or the like is produced from a solid-liquid mixture of water and a carbonaceous component, wherein Treating the solid-liquid mixture at a temperature of more than 1 ° C and more than 5 bar, characterized by: (10) in a film reactor from the 99.  The method of claim 98, wherein the thin film reactor comprises at least one device for solid-liquid separation. 100.  The method of claim 98 or claim 99, wherein at least one of 101 201118162, the solid-liquid separation device comprises a coarse filter and/or a fine filter device or a combination of the two, which can be combined In a filter unit. The method of any one of clauses 98 to 100, wherein: the membrane reactor is used to selectively remove reaction products, products, secondary products, and final products from the reaction mixture, Add or remove precipitates in a controlled manner, or enhance the contact of the precipitates. 102. If the method described in one of the items 98 to 1 of the patent application is applied, the solid-liquid separation of the film reaction 11 is carried out in a continuous manner or in a spaced manner. a method of hydrolyzing and/or producing a material of two itch humus, Maynard or the like in a solid-liquid mixture containing a carbon component, wherein the solid-liquid mixture is treated at a pressure of more than 1 bar at a pressure of more than 5 bar; It is: the first round of wire feeding of the person has 25% to 97% of the solid-potential substance relative to the total volume and is sent in a parallel or branch (Gffset) mode via an i 3% &quot; The method according to the item, wherein the pressure of the vapor pressure of the non-reducible process water is sent by the first conveying line method, wherein the conveying line of the non-pumpable feeder is added to the anti-extruder, Eccentric injection device. Double screw pump, equipped with eCCentnC Spiral PumP, piston pump (piston double screw snail) (or _P_r) or - fruit feed start = ===== method to the middle of the reactor and coating - from the "; = 5 two; send line provides 102 201118162 range of items 103 to 107 of the method, /, medium k The mass yield ratio of the starting material to be added is &amp; 1:2 〇 to 1:5 to 1:1. * One of the items mentioned in item 4 109. For example, the application of patent scopes 1 to 3 to 1 〇 8 laws include the use of other conveyor lines. 110. The method according to any one of the claims 1G3 to 1G9, further comprising using other devices together, such as a storage container, a grinding device, a mixing container, a dosing device, a culture container, a conveying device, Process water container °, heat exchanger or reactor. The method of any one of clauses 103 to 11 wherein the pumping system for conveying the solid-liquid mixture in the first conveying line is designed for a solid content of at least 5% to 10% or 10〇/〇 to 25%. ° 112.  The method of claim 103, wherein the pump for conveying the solid-liquid mixture in the second conveying line is an eccentric screw pump, a spiral displacement (spiral) Displacement) or a piston pump (pist〇n pump) ° 113.  a method for the hydrolysis and/or production of materials or fuels, Maynard or similar reaction products from a solid-liquid mixture of water and carbonaceous components, wherein a temperature of more than 1〇〇1 and a pressure of more than 5 bar The solid-liquid mixture is treated underneath, characterized in that the solid-liquid mixture flows through a heat exchanger for heating, the tube axis having an angle of more than 10 degrees with respect to the horizontal plane. 114.  The method of claim 113, wherein when the solid-liquid mixture passes through the feeding device, the viscosity of the solid-liquid mixture is lowered, and at least a point in the program is lowered to the starting material Three points of viscosity. ''' 115 - a method for feeding a reactor to produce a material or fuel, humus, Maynard or similar reaction product from a solid-liquid mixture of water and a carbonaceous component, wherein at a temperature in excess of 100 ° C and The solid-liquid mixture is treated at a pressure of more than 5 bar, characterized in that: Μ ^ The solid-liquid mixture flows through a heat exchanger to heat the amount of its tube axis relative to the horizontal plane by more than 10 degrees. 103 201118162 116.  For example, one of the 113th to 115th patent applications of the patent scope, this pass at least 117.  For example, in the method of claim 115 or 116, wherein the viscosity is lowered when the heat exchanger is removed, and the solid-liquid 黏 viscosity is reduced to the yarn 2 in the order of the scale: Shen, one of the items 113 to 117 = 'where the solid-liquid mixture has a solid content between 3% and 35% with a solid content between 35% and 60〇/〇 content. The method of any one of clauses 113 to 117, wherein the solid-liquid mixture is introduced into the helium exchanger by a pump. 120. The method of claim 119, wherein the secret to deliver the solid mixture is at least 5% to or from 25% solids. 121. For example, the method described in the ninth or uoth of the Shenqing patent range, wherein the pump for transporting the solid-liquid mixture and/or a backpressure pump is an eccentric screw pump (eccentric) Spiral pump), a spiral displacement or a piston pump 〇122.  a device for treating a solid solution of water and a carbonaceous component at a temperature exceeding 100 ° C and a pressure exceeding 5 bar, comprising a reactor characterized in that: the device comprises a feeding device, Has: a.  - a pump for transporting a solid-liquid mixture having a solids content of at least Μ%; and b.  The heat exchanger has an angle of the tube axis with respect to the horizontal plane greater than 1 degree. 123.  The apparatus of claim 122, wherein the pump is an eccentric spiral pump or a piston pump. 124.  The apparatus of claim 122, wherein the pump is designed to have a pressure of at least 10 to 130 bar. 125.  A device as claimed in any one of claims 122 to 124 wherein the heat exchanger is comprised of at least 60% of vertical tubular members. 104 201118162 126.  The apparatus of the invention of claim 122, wherein the heat exchanger for conveying the solid-liquid mixture is designed to have a solid 3 of 3% to 50/&gt; It is mainly composed of biomass including lignocellulose (1) and/or starch-containing material. 127.  The apparatus of any one of claims 122 to 126, wherein the heat exchanger is designed for the temperature, or at least _2 modules or a unit is used for 2 turns. (: to 300. (: temperature. 128.  The apparatus of any one of claims 122 to 127, wherein the heat exchanger is designed for a pressure of from 1 bar to 12 bar, or at least one module or one unit design At a pressure of 60 to 120 bar. 129.  The apparatus of any one of claims 122 to 128, wherein the hot parent or at least one module or unit is designed for a temperature of up to 25 〇 (: 130.  The apparatus of any one of claims 122 to 129, wherein the hot parent exchanger is in contact with the medium by a heat and a button and a waterproof material, such as a coated metal. , especially for metal, ceramic materials or 珐琅131.  A device according to any one of claims 122 to 130, wherein the tubular member in contact with the medium is made of a durable material. 132.  A device as claimed in any one of claims 122 to 131, wherein the heat exchanger is in contact with the medium in the form of stainless steel, such as austenitic steels or chrome and Steels of Groups 6, 7 and 8 with molybdenum content or duplex steels, copper-recorded alloys, nickel alloys with high molybdenum content. 4610 or titanium. 133.  The apparatus of any one of claims 122 to 132, wherein the heat exchanger is a tubular reactor having a blending system, a pair of tubes, an exchanger, and a tube bundle heat. Exchanger or a plate heat exchanger or a combination of ρ. 134.  The method of claim 122, wherein the heat exchanger is composed of a plurality of similar units and/or has a modular structure: 105 201118162 riding a bicycle, (4) a converter The apparatus of the present invention, as described in claim 137 of the patent application, wherein the layer is passed through the double-walled medium-sized medium-sized medium carrier medium of the tubular reactor, wherein the heat carrier medium The device described in the item ====: wherein the heat carrier ,, the end of the items 138 to 140, the final &amp; degree 2 (4) the heat carrier medium is between _ to war 7:T^tT:m 122 133 where ~..., the parent converter consists of different modules, units or sections. 143.  A device for treating a solid-liquid mixture of water and a carbonaceous component at a temperature exceeding a temperature of more than 5 bar, comprising a reactor, characterized in that the device comprises a hydrolysis device having: a.  - a pump for delivering a solid-liquid mixture having a solids content of at least 10 〇 / 〇 to 15%; and b.  - a heat exchanger having an angle of the tube axis relative to the horizontal plane greater than 1 degree. 144.  The apparatus of claim 143, wherein the hydrolysis apparatus comprises a counterpressure pump. 145.  The apparatus of claim 143 or 144, wherein the pump or the back pressure pump for conveying the solid-liquid mixture is an eccentric spiral pump and a spiral displacement (Spirai) Displacement) or a piston pump. 146.  As described in one of claims 143 to 145, the skirt 106 201118162 is in which the pump or the pressure-resistant pump for conveying the solid-liquid mixture is designed to have a pressure of at least 1 bar to 130 bar. . 147. The apparatus of any one of clauses 143 to 146, wherein the heat exchanger is at least 60. /. The vertical pipe part is constructed. 148. The apparatus according to any one of claims 143 to 147, wherein the heat exchanger for transporting the solid-liquid mixture is for 3% to 5% solids weight, It is mainly designed from biomass including lignocellulose (lign〇cellul〇se) and/or starch-containing materials. - 149.  The apparatus of any one of claims 143 to 148, wherein the heat exchanger is for 60. (: to 30 (TC temperature design, or at least one module or one unit is 2 〇〇. (: to 300X: the temperature is designed. 150.  The apparatus of any one of claims 143 to 149, wherein the heat exchanger is designed for a pressure of 10 to 12 bar, or at least _2 modules or a unit of 60 bar Designed to a pressure of 120 bar. 151.  The apparatus of any one of claims 143 to 15, wherein the heat exchanger or at least one module or unit is for up to 25 inches. The temperature is designed. 152.  The skirt according to any one of the items 143 to 151 of the patent application, wherein the hot contactor is in contact with the medium and is composed of heat-resistant and financial materials and a waterproof material, such as coated metal. Especially for precious metals and ceramic materials. 153.  For example, in the item 143 to 152 of the patent scope, wherein the tube in contact with the medium is composed of a durable material. 154.  The apparatus of any one of claims 143 to 153, wherein the heat exchanger is in contact with the medium by a stainless steel such as austenitic steels or an increase in chromium and molybdenum content. , 7 and 8 steel, $ is composed of duplex steels, copper-nickel alloy, high molybdenum content: gold, such as 2. 4610 or titanium. # σ 155. As set forth in paragraphs 143 to 154 of the patent application, wherein the heat exchanger is a tubular reactor having a blending system, a pair of tubes ^ 107 201118162 a parent exchanger, a bundle bundle heat An exchanger or a plate heat exchanger or a combination of the above. 156. A device as claimed in any one of claims 143 to 153, wherein the heat exchanger is composed of a plurality of similar units and/or has a module: the device described in the item wherein the heat exchange The apparatus of any one of clauses 143 to 157, wherein the module units of the heat exchanger are disposed in a spatially adjacent manner. The scope of the item 143 to 158 of the application, wherein the blending system of the tubular reactor is composed of double walls. 16== The device of claim 159, wherein the thermal energy carrier is intermediate to the double wall of the tubular reactor.糸 Please turn 16th. The device of item wherein the thermal energy carrier medium is hot oil, water vapor or process water. Negative 162. = Please refer to item 143 of the 153th item of the patent, wherein the heat exchanger is designed for different thermal energy carrier media. Clothing 1 Jin 63: ίΓί!, around the 143th to 162th of the items mentioned in the item! The most ί warm ί for the thermal latitude medium between 6 (rc to 350t ^ 164. For example, in the scope of application for patents Nos. 143 to 155, the heat is generated by a different module, unit or zone of two kinds of rotted pigs, water and carbon-containing solid-liquid mixture _ or fuel, buckle , Maynard or a similar reaction product method in which the solid-liquid mixture is treated at a pressure of more than 1 ^ ^ more than 5 bar, characterized in that an enriched process water system portion is used for The starting material t, the liquid mixture produces a bondability, which is used for coating or attaching to the existing starting material in the reaction reactor, as a heat carrier. The medium is used, for example, in the device or as a fertilizer component. One defeated the method described in claim 6 (6), in which the concentration was carried out using a solid-liquid separation method. The method of claim 165, wherein the evaporation of water is used to remove at least 1% to 10% of the water during the agricultural shrinkage in the eighth of the items 165 to 167. In the method of any one of items 165 to 168, the water of at least 1 〇〇/〇 is removed during concentration. 『·ΐί Please request one of the methods described in one of the 165th to 169th patents to be removed directly from the process performed, or used for untreated private water and designed for the sake of pressure - pressure Rong H’s bribes were removed. 171.  The method of any one of claims 165 to 17, wherein the water vapor obtained by evaporation of the process water is used in other parts of the process, for example, for heating before entering the heat exchanger. Starting materials, heating of the hot oil via a heat exchange process and/or means for operating the dried reaction product, such as an air turbulence mill. 172.  - the use of concentrated process water produced by a process for producing materials or fuels, succulent lean, Maynard or similar reactants from a solid-liquid mixture of water and carbonaceous components, wherein the solid-liquid mixture is more than 10% (TC temperature and treatment at a pressure exceeding 5 bar. 'The concentrated process water system is used for: pre-cultivating, preheating the starting material, producing a pumpable solid-liquid mixture, predominating in the reaction mixture, The reactor of the apparatus is coated with or mixed with an existing starting material for returning to the process as a heat carrier medium and/or as a promoter component.  For use as described in claim 172, wherein the process water system is obtained at a temperature of from 1 ° C to 5 (TC) at a temperature in which it is used alone.  For the use described in claim 172, the additional use is 25. 〇 to 5 (TC, 5 (TC to 70 ° C or 7 ° ° C to 99 ° C temperature heating process water. 175.  a device for producing and treating a material or fuel, humus, Maynard or similar reaction product from a solid-liquid mixture of water and a carbonaceous component, wherein it is at a temperature exceeding 100 ° C and exceeding 5 bar The solid-liquid mixture is treated under pressure and is characterized by: 109 201118162 Returning to the solid-state device 'for concentration of the process water and for returning the concentrated process water to the liquid mixture. Also included for solid-liquid separation 176. A device as claimed in claim 175. 177.  The apparatus of claim 175, further comprising an evaporator. 178.  For example, one of the 'devices' of items 175 to 177 of the patent application includes an insulated reservoir for unprocessed process water and formed into a pressure vessel: 179.  - used to produce materials, fuel, humus, Maynard or similar reaction products from a solid-liquid mixture of water and carbonaceous components and at a temperature of more than 1 〇〇〇c and at a pressure of 5 bar The device for processing, characterized in that: the device is as follows: a.  - the feeding device comprises: a compound; / or a pump 'for conveying a solid-liquid mixing father having a solid content of at least 10% to 15 〇 / ,, the angle of the tube axis relative to the horizontal plane is greater than the degree; And less than two anti-fresh 'small--a reaction-like-sense or hybrid system or have a height-to-diameter ratio of at least 2:1. The apparatus of item 179, wherein the heat exchanger comprises the feature of any one of items 53 to 64. Please refer to the equipment of the (10) rhyme of the county, and further include the apparatus of claim 181, wherein the pressure reducing device comprises a reactor with a blending system or a sensor or a combination of the two. 110