WO2011104261A1 - Réacteur pour la carbonisaton hydrothermale de biomasse et procédé permettant de faire fonctionner le réacteur - Google Patents

Réacteur pour la carbonisaton hydrothermale de biomasse et procédé permettant de faire fonctionner le réacteur Download PDF

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Publication number
WO2011104261A1
WO2011104261A1 PCT/EP2011/052654 EP2011052654W WO2011104261A1 WO 2011104261 A1 WO2011104261 A1 WO 2011104261A1 EP 2011052654 W EP2011052654 W EP 2011052654W WO 2011104261 A1 WO2011104261 A1 WO 2011104261A1
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WO
WIPO (PCT)
Prior art keywords
reactor
biomass
line
reaction
inlet
Prior art date
Application number
PCT/EP2011/052654
Other languages
German (de)
English (en)
Inventor
Robert Stöcklinger
Original Assignee
G+R Technology Group Ag
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Application filed by G+R Technology Group Ag filed Critical G+R Technology Group Ag
Publication of WO2011104261A1 publication Critical patent/WO2011104261A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/40—Solid fuels essentially based on materials of non-mineral origin
    • C10L5/44—Solid fuels essentially based on materials of non-mineral origin on vegetable substances
    • C10L5/447—Carbonized vegetable substances, e.g. charcoal, or produced by hydrothermal carbonization of biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining
    • C10L9/086—Hydrothermal carbonization
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Definitions

  • the present invention relates to a reactor for the hydrothermal carbonization of biomass.
  • the reactor is characterized by the fact that it consists of a stainless steel jacket.
  • the reactor is further formed with a first inlet in the upper region of the reactor for a first conduit and at least one outlet in the lower region of the reactor for a third conduit.
  • the first line and the third line are designed such that they can carry a solid / liquid mixture.
  • the invention relates to a method for operating a reactor for the hydrothermal carbonization of biomass.
  • a reaction mixture is first heated.
  • the reaction mixture comprises water, biomass and a copolymerizable substance.
  • the copolymerizable substance is supplied in the preparation of the reaction mixture.
  • the reaction mixture is transferred to a reactor.
  • the reaction takes place at a temperature of 190 ° C to 270 ° C from.
  • the biomass is transferred via a heat exchanger in another reactor in which takes place the copolymerization reaction.
  • German Offenlegungsschrift DE 10 2008 007 791 A1 discloses a device for aqueous charring of biomass and carbonization products obtained thereby.
  • Biomass can be converted to coal by the process of hydrothermal carbonation.
  • Disadvantages of previous methods consist in the high energy consumption for the process cooling and the process start.
  • the efficiency is increased, simplifies the process flow and process reliability can be improved.
  • By using a boiling point suitable coolant energy-saving, automatically dosing, reliable discharge of the process heat is realized as a result of directed Siedeniklauf.
  • a tilt mechanism replaces an agitator and ensures thorough mixing and uniform heat distribution in the process vessel. By storing the process heat of the exothermic process and the use for follow-up processes, external heating is avoided.
  • German Offenlegungsschrift DE 10 2008 028 953 A1 discloses a process for the production of coal from plants and plant residues. For this The raw biomass (wood, plant parts, eg straw, plant residues) is crushed. It wants to achieve a particle size of 5 to 50 mm. The mostly still moist biomass is immersed in a water bath and filled in a pressure-resistant reaction vessel. The container contents are from ambient to the desired reaction temperature, eg. B. 180 ° C, heated. Likewise, the tank pressure is raised to a level above the value corresponding to the evaporation pressure at the set process temperature. During the reaction process, the reaction process enters an exothermic phase where part of the energy chemically bound in biomass is converted to heat.
  • the desired reaction temperature eg. B. 180 ° C
  • the container After the carbonation process has ended (eg 8 to 12 hours, depending on the biomass used and the pressure or reaction temperature), the container is cooled down to the point where a safe pressure reduction to ambient pressure level is possible. The container is then opened and emptied. The coal is filtered from the process water, mechanically dewatered and treated. The reaction vessel is operated intermittently.
  • the hydrothermal reaction proceeds in a high pressure reactor.
  • the reactor is assigned a supply of starting material.
  • the continuous hydrothermal reaction device is a high pressure reaction device.
  • a material supply unit comprising a biomass kneader and pumps so as to transfer the slurry into a tube reactor.
  • the tube reactor consists of
  • the German patent application DE 10 2008 058 44 A1 describes a method and an apparatus for the production of fuels or fuels.
  • the plant or fuels are produced from a solid / liquid mixture of water and a carbon-containing component.
  • the solid / liquid mixture is treated at a temperature of over 100 ° C and a pressure of about 5bar.
  • starting materials are fed via a heat exchanger continuously to a first reactor and the reaction mixture is passed in batches from one to the next reactor and continuously removed reaction products from the last reactor.
  • the reaction space serves to receive a solid / liquid mixture, for example biomass.
  • the reactor has a brewing device with which the solid / liquid mixture can be mixed during treatment and / or processing.
  • European Patent Application EP 1 970 431 A1 also discloses a method and apparatus for the hydrothermal carbonization of biomass.
  • the starting materials are introduced through an inlet into a pressure reactor during an ongoing carbonization process.
  • the reaction products within the reactor are moved from the inlet to the outlet.
  • the biomass converted to a large extent to end products can be removed.
  • International patent application WO 2008 / 059989A1 discloses the hydrothermal carbonization of biomass. It is proposed that a pressure vessel formed substantially as a pipeline with at least one controllable inlet opening and at least one controllable outlet opening is provided with biomass via the at least one controllable inlet opening. Water and / or at least one catalyst can be supplied.
  • the temperature and / or pressure conditions are controlled in the pressure vessel so that the product supplied to the pressure vessel biomass, water and catalyst is transported in the pipeline, wherein biomass, water and catalyst react with each other and at least one controllable outlet at least one reaction product of Contents is taken.
  • International Patent Application WO 2008/193309 discloses a method for converting biomass into higher energy density solids, especially coal, humus or peat.
  • organic substances from the biomass are slurried to form a suspension in water, and a part of the suspension to be converted is heated to a reaction temperature and converted at elevated pressure by hydrothermal carbonation into the higher energy density solids.
  • the method is characterized in that the conversion is carried out in a reaction volume that is below the surface of the earth.
  • European Patent Application EP 2 130 893 A2 discloses a method for producing coal, in particular coal sludge.
  • the coal slurry is made from moist biomass, in particular sewage sludge by hydrothermal carbonization, wherein the carbon structure of the biomass is preferably broken at at least 180 ° C to 200 ° C with exclusion of air.
  • the process proceeds in particular in batch mode, wherein the biomass is concentrated by dehydration to values above 10% dry matter content before the hydrothermal carbonization. Before the hydrothermal carbonization, the biomass is brought to a pH ⁇ 4.
  • the process waste heat generated during the hydrothermal carbonization is used for the subsequent drying of the resulting product.
  • Dosing devices, pumps and valves are used to feed parallel reactors.
  • the reactors have a reaction to improve the reaction Agitator.
  • tubular reactors can be used which ensure a good mixing of the sewage sludge.
  • biomass In contrast to fossil fuels, biomass comprises renewable raw materials, which are available as domestic energy sources in the long term, as well as all liquid and solid organic substances and products of biological and biochemical processes and their transformation products, which have a sufficiently high carbon content for this process and otherwise in their Composition and nature of economically useful reaction, intermediate, by-products and end products can be processed by the hydrothermal carbonization to fuels.
  • the starting materials include carbohydrates, sugars and starches, agricultural and forestry products, as well as specially grown energy crops (fast-growing tree species, reed grasses, cereal crops, etc.), soybeans, sugarcane and cereal straw, as well as biogenic residues, wastes and by-products.
  • Plant and plant remains of other origin (roadside greenery, landscape care goods, etc.), agricultural waste including straw, sugar cane leaves, Abputzgetreide, unsellable batches of potatoes or sugar beet, spoiled silage, and other leftovers, grass clippings, cereal straw, beet leaves, sugar cane leaves, carbonaceous residual and Waste materials, including biowaste, high-calorific fractions of domestic and commercial waste, sewage sludge, various types of wood and classes, including forest wood, timber, pallets, used furniture, sawdust, food and waste residues, including food industry kitchen and food waste, garbage, old fats, as well as paper and pulp, textiles in particular from natural fibers and natural polymers and animal excreta, including manure, horse manure and poultry droppings.
  • agricultural waste including straw, sugar cane leaves, Abputzgetreide, unsellable batches of potatoes or sugar beet, spoiled silage, and other leftovers, grass clippings, cereal straw, beet leaves, sugar cane leaves, carbonaceous residual and
  • a device for the treatment of biogenic residual masses which comprises a cylindrical reactor, in the food waste u. ⁇ . Be subjected to a temperature-pressure hydrolysis.
  • the reactor is designed as a loop reactor with a heatable jacket surface. By means of a pump, a flow is generated within the reactor, which ensures thorough mixing of the suspension.
  • the invention has for its object to provide a reactor for the production of carbonaceous products from biomass by means of hydrothermal carbonation, which ensures a high production reliability and Störunan memorikeit.
  • the object is achieved by a reactor comprising the features of claim 1. It is a further object of the present invention to provide a method of operating a reactor for the production of carbonaceous products from biomass by means of hydrothermal carbonation, the method providing high production safety and susceptibility to interference.
  • the reactor for the production of carbonaceous products from biomass by hydrothermal carbonation is constructed of a stainless steel shell.
  • the reactor has a first inlet at the top of the reactor for a first conduit and at least one outlet at the bottom of the reactor for a third conduit.
  • the reactor further has a second inlet in the upper region of the reactor.
  • the second inlet is connected to the outlet via a second conduit.
  • the second conduit is provided with a heat exchanger and a pump so that the reacting solid / liquid mixture in the reactor can be pumped controlled via the outlet and the second inlet.
  • at least one stirrer is provided in the reactor.
  • a three-way valve is provided in the area of the outlet.
  • the third conduit it is possible to provide for the discharge of the reaction products from the reactor when the process of hydrothermal carbonization of the biomass in the reactor is completed.
  • the reactor is also associated with a plurality of sensors that determine a plurality of process parameters, such as pressure, temperature, pH and / or level inside the reactor.
  • process parameters such as pressure, temperature, pH and / or level inside the reactor.
  • the values of the process parameters determined by the sensors are transferred to the process control so that the parameters during a reaction process in the reactor are within a predefined fluctuation range via a suitable control.
  • the reactor is further provided with a control device by means of which a predefined pressure level inside the reactor can be adjusted by means of a two-way valve during the process of hydrothermal carbonization of biomass.
  • the reactor according to the invention is integrated in a system.
  • the plant for the production of carbonaceous products from biomass by means of the hydrothermal carbonization comprises a first area, in which the provision, reduction and mixing of different types of biomass is carried out.
  • possible biomass containing some carbon can be processed.
  • the processing and preparation of the mixed biomass takes place.
  • water and a catalyst is added to adjust the required for the subsequent reaction process proportion of the dry matter in the reaction mixture.
  • the second area is followed by a third area, in which the implementation of the reaction process according to the hydrothermal carbonation takes place.
  • the third area is followed by a fourth area, which serves to further process the reaction products.
  • the third area consists of at least three reactors, all of which are identical.
  • Each of the at least three reactors has a stirrer inside, thus improving the mixing and circulation of the biomass.
  • an agglomeration of the reaction products of biomass on the inner walls of the reactor is avoided.
  • the at least three reactors are interconnected via a first line system, a second line system and a third line system.
  • the first conduit system is guided via a first heat exchanger, so that at least one of the at least three reactors can be controlled and selectively filled with biomass from the second region.
  • the second line system is also passed through a heat exchanger.
  • a pump is provided in the second line system so that biomass in the reaction process can be controlled from the active reactor of the at least three reactors and selectively circulated during the reaction process.
  • the pump thus achieves good mixing of the reaction products in the active reactor of the at least three reactors.
  • a third line system is led from the at least three reactors via a heat exchanger.
  • the reaction products of the completed reaction process are withdrawn from the active reactor and fed via a relaxation device the fourth area.
  • the reaction products are only withdrawn from the active reactor when the reaction process in the active reactor has come to a standstill.
  • the at least three reactors of the third region are operable in such a way that at least one reactor is the active reactor.
  • At least one other reactor is the reactor that is being filled with the added biomass from the second area.
  • At least one further reactor is the reactor being emptied. This reactor was the previous active reactor, in the reaction process has come to a conclusion, so that its content can be transferred to the further treatment of the reaction products in the fourth area.
  • the first line system, the second line system and the third line system are provided with a plurality of controllable two-way valves and a plurality of controllable three-way valves.
  • the entire hydrothermal carbonization plant is connected to a program control so that the specific filling, circulation and discharge of the at least three reactors in the third area can be regulated or controlled.
  • the first area for the provision, crushing and mixing of at least one type of biomass comprises a multitude of acceptance and storage positions for the unmixed provision of the different types of biomass.
  • at least one comminution unit and a mixer for the different biomasses are provided.
  • the comminution unit is necessary in order to produce the biomass to a required particle size or a range of the process-usable particle sizes of the biomass.
  • the second area has a mixing tank in which the comminuted and mixed biomass is filled.
  • the comminuted and mixed biomass is further added via a line with process water.
  • a catalyst required for the reaction process of the hydrothermal carbonization can be added to the process water.
  • the process water and the catalyst are fed together via a mixer.
  • An agitator operated by a motor is provided in the mixing vessel in order to ensure good mixing of the biomass with the process water and the catalyst. In addition, by means of the agitator, a settling of the biomass at the bottom of the mixing container avoids.
  • the added amount of process water to the mixed and comminuted biomass can thus adjust the proportion of dry matter in the reaction process, which takes place downstream in at least one of the reactors.
  • the mixing container In the mixing container to set a dry matter content of 20% to 60%.
  • the proportion of the dry substance depends essentially on the fraction of the various types present in the comminuted and mixed biomass and the resulting reaction processes in the downstream reactors.
  • the biomass mixed with process water and catalyst reaches the third area via a third line, in which the reaction process is carried out.
  • a pump is provided so as to be able to adjust the filling rate of the at least one reactor in the third range.
  • a collecting vessel for receiving the reaction products from the at least one reactor is provided for further processing of the reaction products, from which the reaction products are removed.
  • the reaction products are only then removed from the initially active reactor, after which the reaction process is completed in this reactor.
  • the collecting container also has a motor operated agitator. Via a pumped line, the reaction products are fed to a dehydrator and a downstream dryer.
  • a line leads to a collecting container for the process water obtained in the dewatering device.
  • the process water is returned to the second area via a line provided with a pump.
  • the process water can in turn be introduced into the reaction cycle.
  • the process water is thus fed to the mixed and comminuted biomass in the mixing container provided in the second area.
  • the reaction product is after the Drying process removed from the dryer and fed to a collection container. From the collection of packaging or removal can be organized.
  • a fifth region may be provided. At least a portion of the reaction products from the at least one active reactor may be fed directly to the fifth region.
  • reaction products are, as already mentioned above, only taken from the at least one active reactor, if in this the reaction process has been completely completed. These reaction products, which are supplied to the fifth region, have a dry matter content of about 10%.
  • carbon dioxide is added to the reaction products.
  • the carbon dioxide comes z. B. from the coal combustion of a fossil power plant. Any combustion process that produces carbon dioxide can be used as a carbon dioxide source. Carbon dioxide can thus be supplied to the fifth region of the plant and is thus involved in the production of synthesis gas.
  • the plant is in the first area, in the second area, in the third area, in the fourth area and in the fifth area a variety of controllable two-way valves and three-way valves, thereby regulating a material flow within the plant via a central program control, or can be adjusted.
  • the plant can be used to produce coal and / or synthesis gas as a reaction product. It is possible by appropriate program control to adjust the reaction product to the needs of a customer so that the fuel is an optimal performance during combustion.
  • the setting and additional elements of the coal contained in the fuel can be adjusted to the reaction process by suitable selection of the starting products of the various biomass types.
  • the method of operating a reactor for the production of carbonaceous products from biomass by means of hydrothermal Carbonization comprises at least one reactor comprising a first inlet in the upper region of the reactor for a first line and at least one outlet in the lower region of the reactor for a third line. About the first line and the third line, a solid / liquid mixture of biomass can be performed.
  • the biomass reacting in the reactor is circulated during the reaction process by means of a second line from the outlet to the second inlet in the upper region of the reactor.
  • the reaction process taking place in the reactor is monitored by means of several sensors and values of the various process parameters are determined.
  • the various values of the process parameters are transmitted to a program controller, which keeps the process parameters of the reaction process in the reactor in the range of a predefined fluctuation range.
  • a program controller which keeps the process parameters of the reaction process in the reactor in the range of a predefined fluctuation range.
  • at least one stirrer is provided in the reactor.
  • the reacting in the reactor biomass is guided by means of the second line by a pump via a heat exchanger.
  • energy is withdrawn from the exothermically reacting biomass in the reactor so that a reaction temperature prevailing in the reactor is kept within a predefined fluctuation range.
  • the reaction products taken from the reactor (the reaction process is completed in the reactor so that it can be emptied) of the third area have a dry matter content of about 10%.
  • a dry matter content of about 50% is set.
  • a dry matter content of about 90% is achieved.
  • the biomass is constantly circulated via a heat exchanger. After completion of the reaction process in the At least one active reactor, the biomass is discharged from the reactor and thereby fed via a third heat exchanger and a relaxation device the fourth area.
  • a fifth region can also be provided in the system in which at least part of the reaction products can be supplied from the active reactor after completion of the reaction process. It is also possible that all of the reaction products withdrawn from the active reactor are fed to the fifth region. Synthesis gas is generated in the fifth area.
  • a program control controls the material flow within the system for carrying out the method.
  • a fuel can be produced, which is carbonaceous.
  • the fuel can be a coal.
  • the fuel may be synthesis gas.
  • FIG. 1 shows a schematic representation of the invention
  • FIG. 2 shows a schematic view of a device according to the invention
  • Reactor as used in the hydrothermal carbonization of biomass.
  • FIG. 3 shows a schematic representation of the first region of the hydrothermal carbonization plant in which the different biomasses required for the reaction process can be comminuted and mixed.
  • FIG. 4 shows a schematic representation of the second region of FIG. 3
  • Plant for hydrothermal carbonation in which the comminuted and mixed biomass with process water and catalyst be added before they are fed to the reaction process.
  • Figure 5 shows a schematic representation of the third area, in which at least three reactors are provided, which are connected to each other via different lines.
  • Figure 6 shows a schematic representation of the elements of the fourth
  • FIG. 1 shows the schematic structure of the plant 1 for hydrothermal carbonization.
  • the hydrothermal carbonization unit 1 is formed from a first area 100, a second area 200, a third area 300, and a fourth area 400.
  • the first area 100, the second area 200, the third area 300 and the fourth area 400 are connected by means of a common program control 10.
  • the first area 100 the compilation and mixing of the different biomasses takes place.
  • the thus mixed and comminuted biomasses reach the second region 200, in which a processing and preparation of the mixed biomasses is carried out.
  • Process water PW is added to the crushed and mixed biomasses.
  • the biomass mixed with process water PW reaches the reactor region, which is referred to as the third region.
  • the reaction process of the hydrothermal carbonization In the third area, the reaction process of the hydrothermal carbonization.
  • the finished reaction product is supplied to the fourth area where processing of the reaction products of the hydrothermal carbonization process is performed.
  • process water PW is recovered, which is ultimately returned to the second area for reuse.
  • FIG. 2 shows a simplified schematic representation of the active reactor 301 A in connection with the second line 321, which is formed as a loop line or switchable to a ring line.
  • the loop is obtained by suitable control of two-way valves 32 and / or three-way valves 33 of the system 1 for hydrothermal carbonization.
  • the second line 321 (or the controlled loop formed) comprises the second heat exchanger 320.
  • the biomass which is currently reacting is continuously circulated via the second heat exchanger 320 by means of a pump 30 and the second line 321.
  • At least one stirrer 350 is provided in the reactor 301, thereby achieving an additional thorough mixing and circulation of the reacting biomass 5-i, 5 2 , 5 n .
  • each reactor 301 for the production of carbonaceous products from biomass 5-i, 5 2 , 5 n by means of hydrothermal carbonation has a stainless steel jacket.
  • the reactor 301 has a first inlet 21 in the upper region 301 o of the reactor 301 for a first conduit 31 1.
  • the reactor 301 has formed at least one outlet 23 in the lower region 301 u for a third line 331, the first line 31 1 and the third line 331 leading a solid / liquid mixture.
  • the reactor 301 has a second inlet 22 in the upper region 301 o of the reactor 301 and the second inlet 22 is connected to the outlet 23 via a second line 321 or interconnected within the system 1 such that the second line 321 controls the inside Reacting biomass of the respective reactor 301 from the outlet 23 to the second inlet 22 leads.
  • the second conduit 321 is provided with a heat exchanger 320 and a pump 30, whereby the solid / liquid mixture in the reactor 301 can be circulated via the outlet 23 and the second inlet 22.
  • a weir 350 is provided in the reactors 301, which is preferably arranged in the lower region of the reactors 301.
  • the reactor 301 is assigned a plurality of sensors 25, which determine a multiplicity of process parameters during the reaction process in the reactor 301.
  • the process parameters may be pressure, temperature, pH, and / or level inside the reactor 301, etc.
  • the measured values of the parameters are fed to the program controller 10 of the system 1, which by means of controllable two-way valves 32 or three-way valves 33 a predefined pressure level inside the reactor (301) or the material flow during the process of hydrothermal carbonization of biomass 5 ; 5 2 , 5 n .
  • reactors 301 may take on different functions depending on the end of the production process.
  • at least one reactor 301 may be the active reactor 301 A. If the reaction process is completed, the previously at least one active reactor 301 A is the emptying reactor 301 L. If the at least one emptying reactor 301 L is completely emptied, the reactor 301 becomes the fillable reactor 301 F.
  • the number of reactors 30, the active reactors 301 A or emptying reactors 301 L or refillable reactors 301 F are dependent on the process conditions to ensure a continuous output of reaction products from Appendix 1.
  • FIG. 3 shows a schematic representation of the first region 100 of the plant 1 for the hydrothermal carbonization of biomass.
  • the first area comprises a plurality of acceptance and storage locations 12 ; 12 2 , 12 n for the different types of biomass 5-i, 5 2 , 5 n .
  • the embodiment of the region 100 shown in FIG. 4 represents only one possible form of embodiment and should not be construed as a limitation. It is obvious to a person skilled in the art that the first area 100 can be designed according to the customer's requirement.
  • the number of acceptance and storage locations 12 ; 12 2 , 12 n depends on the different types of biomass that are to be processed in Appendix 1. Likewise, the number of comminution units 13 depends on the type of biomass that is to be processed with the system 1. After the corresponding comminution of the biomasses, these are fed to a mixer 14, in which the mixed biomass 5N is made available for the further reaction process.
  • a first comminution unit 13i and a second comminution unit 13 are 2 intended.
  • the first crushing unit 13 is designed as a crusher.
  • the second crushing unit 13 2 is designed as a hammer mill.
  • the first crushing unit 13i are thus supplied with large pieces of biomass, which still require a high degree of comminution before they are fed to the mixer.
  • the second crushing unit 13 2 is designed as a hammer mill and thus can already shredded parts of biomass, such.
  • B. Strohab mount, grass clippings, bark waste, wood chips, etc. continue to shred and feed them directly to the mixer 14.
  • an acceptance and storage point 12 3 for already liquid biomass is present. This liquid biomass can z. B.
  • the biomass comminuted with the first comminuting unit 13i is thus supplied to a feed line of the liquid biomass from the receiving and storing point 12 3 .
  • the biomass coming from the first comminution unit 13 is already mixed with a liquid biomass before it reaches the mixer 14.
  • the biomass passes via a line 1 1 1 in the second area 200.
  • the second area 200 of the system 1 comprises a mixing container 21st In the mixing vessel 21, a stirrer 220 driven by a motor 221 is provided.
  • the mixing vessel 21 passes through the line 1 1 1, the mixed biomass 5N.
  • the process water PW is supplied to the mixing vessel 21 via a line 21 1.
  • a mixer 214 is inserted. Before the process water PW passes via the line 21 1 in the mixer, opens into the line 21 1, a line 212 which feeds a catalyst from a tank 213 in the process water.
  • the catalyst may, for. For example, formic acid, citric acid or sulfuric acid.
  • the mixture thus obtained which has a dry matter content of 20% to 60%, via a line 222, which is provided with a pump 30, the third area 300th fed.
  • a plurality of two-way valves 32 is provided. These two-way valves 32 are connected to the program controller 10. Thus, it is possible by targeted control of the two-way valves to control the flow of material targeted and thus z. B. to set the dry matter content in the mixing container 21 targeted.
  • the size of the dry matter content depends essentially on the downstream process conditions in the third range.
  • the structure of the third region 300 is shown schematically in FIG.
  • the third region 300 comprises at least three reactors 301.
  • Each of the reactors is provided with a positive pressure line 302 which terminates in a controllable two-way valve 32.
  • the pressure inside the reactor can thus be adjusted to a predefined level. It is also possible to release the pressure if, in the interior of the at least one reactor 301, the pressure rises above a predefined level.
  • At least three reactors 301 must be present to ensure continuous production of the reaction products of the hydrothermal carbonation process.
  • At least one reactor 301 of the reactors is an active reactor 301 A.
  • active reactor means that in this reactor 301, the process of hydrothermal carbonization takes place and is not yet completed.
  • At least one other reactor 301 of the at least three reactors biomass is introduced via a line 31 1 in the reactor 301.
  • This reactor 301 is referred to as fillable reactor 301 F.
  • the fillable reactors 301 F are filled via line 31 1 with the mixed with process water and catalyst biomass.
  • a first heat exchanger 310 is introduced in line 31 1, a first heat exchanger 310 is introduced in line 31 1, a first heat exchanger 310 is introduced.
  • the line 31 1 connects all the reactors 301 of the third area 300.
  • a controllable three-way valve 33 thus the line 31 1 can be released in the direction of at least one refillable reactor 300F, so that the reactor 301 F can be filled with biomass, process water and catalyst.
  • a second line system 321 is provided, which likewise connects each reactor 301 of the third area 300 to one another.
  • the second line 321 is designed as a ring line and is also guided via a second heat exchanger 320.
  • a pump 30 is provided in the line 321, with which the biomass from the at least one active reactor 301 A is constantly pumped through the second heat exchanger 320. By this pumping to achieve a constant mixing of the biomass in the active reactor 301 A.
  • a plurality of three-way valves 33 and two-way valves 32 are provided, thus the material flow of just in the active reactor 301 A reacting biomass via the loop 321 and the heat exchanger to pump.
  • the two-way valves 32 and the three-way valves 33 are controlled such that the second line 321 with the at least one active reactor 301 A forms an open ring, so that the pumping of the biomass during the reaction process in the active reactor 301 A is possible.
  • At least one further reactor 301 of the reactors in the third region 300 is a reactor 301 which is currently being emptied.
  • This reactor 301l which is currently able to empty, was previously the active reactor 301 A.
  • the active reactor 301 A then becomes the empty reactor 301 L.
  • Each of the reactors 301 is connected to a third line 321, which is passed through a third heat exchanger 320.
  • a plurality of two-way valves 32 and three-way valves 33 are also provided, thus controlled to connect the empty reactor 301 L to the third conduit 331.
  • the withdrawn from the empty reactor 301 L reaction product is connected by means of the third line 331 via a Relaxation device 340 guided so that the reaction products are brought substantially to an ambient pressure level. From the expansion device 340, the reaction products reach the fourth region 400 and / or the fifth region 500, in which, as already mentioned, synthesis gas can be produced.
  • the fifth region 500 is omitted, in which synthesis gas can be prepared from the reaction products in conjunction with carbon dioxide.
  • the reaction product now passes via the line 331 in the fourth area and is spent there in a collecting container 41.
  • a stirrer 420 which is driven by a motor 421, is arranged.
  • the reaction product is transferred to a dewatering device.
  • the reaction products fed in via line 331 have a dry matter content of about 10%.
  • the dehydrator 430 the dry matter content is increased to about 50%.
  • the process water PW obtained from the reaction products passes into a collecting container 436. Should the level in the collecting container 436 become too high, the excess process water PW is discharged via an overflow 437 to the environment. Via the line 31 1, which is provided with a pump 30 and a two-way valve 32, the process water PW is returned to the second area 200 of the system 1.
  • the reaction product passes into a dryer 432.
  • the dryer is driven by a motor 433.
  • the dry matter content of the reaction products is increased to about 90%.
  • the dried reaction product passes into a collecting container 434. From the collecting container 434, the distribution to the consumers of the reaction products prepared with the plant 1 can finally take place.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

L'invention concerne un réacteur (301) et un procédé permettant de faire fonctionner le réacteur (301) pour la préparation de produits carbonés à partir de biomasse (51, 52,..., 5n) par carbonisation hydrothermale. Le réacteur (301) est constitué d'une enveloppe en acier spécial et comporte un premier orifice d'entrée (21) dans la zone supérieure (301o) du réacteur (301) pour un premier conduit (311) et au moins un orifice de sortie (23) dans la zone inférieure (301U) du réacteur (301) pour un troisième conduit (331). Le réacteur (301) comporte un second orifice d'entrée (22) dans la zone supérieure (301o) du réacteur (301). Le second orifice d'entrée (22) est raccordé à l'orifice de sortie (23) via un second conduit (321). Le second conduit (321) intègre un échangeur de chaleur (320) et une pompe (30), le mélange solide/liquide présent dans le réacteur (301) pouvant être transvasé à la pompe par l'intermédiaire de l'orifice de sortie (23) et du second orifice d'entrée (22). Au moins un agitateur (350), intégré dans le réacteur (301), sert également au mélangeage et à la recirculation de la biomasse (51, 52,..., 5n).
PCT/EP2011/052654 2010-02-26 2011-02-23 Réacteur pour la carbonisaton hydrothermale de biomasse et procédé permettant de faire fonctionner le réacteur WO2011104261A1 (fr)

Applications Claiming Priority (2)

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DE102010000578A DE102010000578A1 (de) 2010-02-26 2010-02-26 Reaktor zur hydrothermalen Karbonisierung von Biomasse und Verfahren zum Betrieb des Reaktors
DE102010000578.9 2010-02-26

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3753999A1 (fr) * 2019-06-19 2020-12-23 The Hong Kong Research Institute of Textiles and Apparel Limited Système de réaction hydrothermique semi-continu

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2013117000A1 (fr) * 2012-02-09 2013-08-15 同济大学 Système et procédé mettant en oeuvre une réaction hydrothermique
CN104650935B (zh) * 2015-02-11 2017-02-01 中原工学院 一种生物质有效的处理方法
CN105688787B (zh) * 2016-03-29 2019-02-12 范秀磊 一种无噪音污染的反应釜
CN109351297B (zh) * 2018-11-29 2023-10-17 清华大学 一种水热反应系统及其运行方法
IT201800020320A1 (it) * 2018-12-20 2020-06-20 Daniele Basso Impianto e procedimento per la trasformazione di biomassa

Citations (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19723510C1 (de) 1997-06-05 1999-02-18 Atz Evus Verfahren und Vorrichtung zur Behandlung biogener Restmassen
US6090978A (en) * 1996-07-19 2000-07-18 Met-Rx Usa, Inc. Process for manufacturing 3-hydroxy-3-methylbutanoic acid
WO2008019309A1 (fr) 2006-08-04 2008-02-14 Metabasis Therapeutics, Inc. Nouveaux inhibiteurs du fructose 1,6-bisphosphatase
WO2008059989A1 (fr) 2006-11-15 2008-05-22 Toyota Boshoku Kabushiki Kaisha Ensembles matrices de poinçonnage à cisaillement
WO2008081407A2 (fr) 2006-12-28 2008-07-10 Schweiger, Martin Matériau et/ou combuistible produit à partir de biomasse
EP1970431A1 (fr) 2007-03-13 2008-09-17 Loritus GmbH Dispositif et procédé de carbonisation hydrothermale de biomasses
DE102008005844A1 (de) 2007-02-08 2008-10-02 Wienert, Volker, Prof. Dr. Gummiring zur Therapie des Hämorrhoidalleidens und Verfahren zu seiner Herstellung
WO2008120662A1 (fr) 2007-03-30 2008-10-09 B Food Science Co., Ltd. Appareil de réaction hydrothermale haute pression continue pour un traitement de biomasse
DE102008007791A1 (de) 2008-02-06 2009-08-27 Kleiner, Söhnke Vorrichtung und verbessertes Verfahren zur wässrigen Verkohlung / hydrothermalen Karbonisierung von Biomasse sowie dadurch erhaltene Karbonisierungsprodukte
EP2130893A2 (fr) 2008-06-05 2009-12-09 TerraNova Energy GmbH & Co. KG Procédé de fabrication de charbon, notamment de boue de charbon
DE102008026991A1 (de) * 2008-06-05 2009-12-10 Marc Buttmann Verfahren zum Herstellen von Kohle insbesondere von Kohleschlamm
DE102008028953A1 (de) 2008-06-18 2009-12-24 Hydrocarb Gmbh & Co. Kg Verfahren zur Erzeugung von Kohle aus Pflanzen und Pflanzenresten
WO2010006881A1 (fr) 2008-06-23 2010-01-21 Csl Carbon Solutions Ltd. Procédé de préparation d’un matériau hybride hydrothermal à partir d’une biomasse, et matériau hybride hydrothermal pouvant être obtenu par le procédé

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE69117871T2 (de) * 1990-10-31 1996-11-07 Nippon Petrochemicals Co Ltd Verfahren zur Herstellung eines Niedrigalkylacetats
DE10201689A1 (de) * 2002-01-17 2003-07-31 Merck Patent Gmbh Kontinuierliches Verfahren zur Hydrolyse einer lösungsmittelhaltigen organischen Verbindung

Patent Citations (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6090978A (en) * 1996-07-19 2000-07-18 Met-Rx Usa, Inc. Process for manufacturing 3-hydroxy-3-methylbutanoic acid
DE19723510C1 (de) 1997-06-05 1999-02-18 Atz Evus Verfahren und Vorrichtung zur Behandlung biogener Restmassen
WO2008019309A1 (fr) 2006-08-04 2008-02-14 Metabasis Therapeutics, Inc. Nouveaux inhibiteurs du fructose 1,6-bisphosphatase
WO2008059989A1 (fr) 2006-11-15 2008-05-22 Toyota Boshoku Kabushiki Kaisha Ensembles matrices de poinçonnage à cisaillement
WO2008081407A2 (fr) 2006-12-28 2008-07-10 Schweiger, Martin Matériau et/ou combuistible produit à partir de biomasse
DE102007062808A1 (de) * 2006-12-28 2008-07-17 Dominik Peus Vorrichtung zur Behandlung von Fest-/Flüssiggemischen
DE102008005844A1 (de) 2007-02-08 2008-10-02 Wienert, Volker, Prof. Dr. Gummiring zur Therapie des Hämorrhoidalleidens und Verfahren zu seiner Herstellung
EP1970431A1 (fr) 2007-03-13 2008-09-17 Loritus GmbH Dispositif et procédé de carbonisation hydrothermale de biomasses
WO2008120662A1 (fr) 2007-03-30 2008-10-09 B Food Science Co., Ltd. Appareil de réaction hydrothermale haute pression continue pour un traitement de biomasse
DE102008007791A1 (de) 2008-02-06 2009-08-27 Kleiner, Söhnke Vorrichtung und verbessertes Verfahren zur wässrigen Verkohlung / hydrothermalen Karbonisierung von Biomasse sowie dadurch erhaltene Karbonisierungsprodukte
EP2130893A2 (fr) 2008-06-05 2009-12-09 TerraNova Energy GmbH & Co. KG Procédé de fabrication de charbon, notamment de boue de charbon
DE102008026991A1 (de) * 2008-06-05 2009-12-10 Marc Buttmann Verfahren zum Herstellen von Kohle insbesondere von Kohleschlamm
DE102008028953A1 (de) 2008-06-18 2009-12-24 Hydrocarb Gmbh & Co. Kg Verfahren zur Erzeugung von Kohle aus Pflanzen und Pflanzenresten
WO2010006881A1 (fr) 2008-06-23 2010-01-21 Csl Carbon Solutions Ltd. Procédé de préparation d’un matériau hybride hydrothermal à partir d’une biomasse, et matériau hybride hydrothermal pouvant être obtenu par le procédé

Non-Patent Citations (5)

* Cited by examiner, † Cited by third party
Title
ANGEW. CHEMIE, vol. 45, 1932, pages 517 - 519
E. BEHRL ET AL., ANN. CHEM., vol. 493, 1932, pages 97 - 123
J.P. SCHUHMACHER ET AL., FUEL, vol. 39, 1960, pages 223 - 234
Q. WANG ET AL., CARBON, vol. 39, 2001, pages 2211 - 2214
X. SAN; Y. LI, ANGEW. CHEM. INT. ED., vol. 43, 2004, pages 597 - 601

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3753999A1 (fr) * 2019-06-19 2020-12-23 The Hong Kong Research Institute of Textiles and Apparel Limited Système de réaction hydrothermique semi-continu

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