WO2008138637A2 - Procédé et dispositif de carbonisation hydrothermale (htc) de biomasse à l'aide d'une installation htc - Google Patents

Procédé et dispositif de carbonisation hydrothermale (htc) de biomasse à l'aide d'une installation htc Download PDF

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Publication number
WO2008138637A2
WO2008138637A2 PCT/EP2008/003932 EP2008003932W WO2008138637A2 WO 2008138637 A2 WO2008138637 A2 WO 2008138637A2 EP 2008003932 W EP2008003932 W EP 2008003932W WO 2008138637 A2 WO2008138637 A2 WO 2008138637A2
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WO
WIPO (PCT)
Prior art keywords
reactor
pressure
temperature
water
biomass
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PCT/EP2008/003932
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German (de)
English (en)
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WO2008138637A3 (fr
Inventor
Tobias Wittmann
Hans-Joachim Von Massow
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Suncoal Industries Gmbh
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Priority claimed from DE102007022840A external-priority patent/DE102007022840A1/de
Application filed by Suncoal Industries Gmbh filed Critical Suncoal Industries Gmbh
Publication of WO2008138637A2 publication Critical patent/WO2008138637A2/fr
Publication of WO2008138637A3 publication Critical patent/WO2008138637A3/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
    • 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
    • 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
    • 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

  • a first inventive concept consists in a method and a device for controlling the preheating of biomass and cooling a reaction for hydrothermal carbonization (HTC) of biomass, wherein an HTC reactor via at least one pressure and / or temperature-controlled valve water vapor is removed, which subsequently can be used for preheating.
  • HTC hydrothermal carbonization
  • a second aspect of the invention consists in a method for the separation of the product mixture following a hydrothermal Karbonmaschinesretress in a HTC system without prior relaxation to ambient pressure to perform the separation efficiently and can lead the separated water in a circle and reuse.
  • a method of utilizing the heat of reaction of an HTC reaction to evaporate the water discharged from the HTC plant to produce a liquid fertilizer.
  • the reaction of the hydrothermal carbonization converts biomass into humus or coal and water in an exothermic reaction between about 180 0 C and 230 0 C biomass.
  • the above-mentioned temperature window must be maintained for about four hours, then the temperature must be kept constant at about 180 0 C between four and seven hours.
  • hypothermia the biomass reacts only partially, overheating causes unwanted by-products.
  • CONFIRMATION COPY Heat exchanger or heating and cooling coils is realized.
  • the geometry of the reactor is further limited by the design of the heat exchanger.
  • the resulting heat of reaction can not be used for an efficient preheating of the biomass beyond, since the temperature range in which the reaction takes place is too small to provide the necessary for a heat transfer with compact heat exchangers temperature differences, or a possibly necessary Temperature increase between reactor and preheater easy to implement.
  • the object of the invention to find a solution for the economic implementation of the hydrothermal carbonization of biomass and to eliminate the known disadvantages of process control with the help of heating or cooling coils.
  • the necessary uniformity in the preheating of the biomass, the cooling during the conversion process and the temperature during post-processing - and thus an efficient reaction control - achieved in that a controlled steam extraction takes place from the reactor and this steam then preferably for preheating the biomass in a preheater and temperature maintenance in a post-processor is introduced. Since the boiling temperature and the boiling pressure of the reacting mixture can not be selected independently of each other and energy must be expended for evaporation, the pressure reduction associated with removal of water vapor from the reactor triggers evaporation. The heat required for this purpose is removed from the reaction mixture and leads to a lowering of the temperature.
  • water vapor is thus removed from the reactor in order to control the internal reactor temperature of a reactor for the continuous or discontinuous hydrothermal carbonization of biomass.
  • the water vapor can then be used to preheat the biomass.
  • a pressure increase can take place between a preheater and the reactor. If the reaction regime requires a higher pressure or a higher temperature in the preheater than in the reactor, a pressure reduction must take place between the preheater and the reactor.
  • the steam needs then first compressed and then introduced into the preheater.
  • the steam extraction can be done via pressure and / or temperature controlled valves
  • Another object is to find a solution for the economic separation of the reaction products of the hydrothermal carbonization of biomass and thereby overcome the known disadvantages of thermal drying, mechanical, thermal or mechanical-thermal dewatering.
  • the product mixture is not relaxed to ambient pressure as soon as it reaches the desired quality, but is squeezed out at high temperature and pressure. Due to the pressure maintenance, the evaporation of the water present in the product and the associated lowering of the temperature of the mixture is at least partially avoided. Since the reaction mixture exits the reactor at a high temperature and under high pressure, the heating and heat recovery necessary in a mechanical-thermal dehydration are partially or completely avoided and the efficiency of separation is increased.
  • the water thus separated may preferably be circulated and admixed with the biomass prior to or during the reaction.
  • An admixture is made with the aim of a) increasing the heat capacity of the reaction mixture in order to better control the time of removal of the heat of reaction by means of a steam extraction from the reactor, b) the complete envelopment of the biomass with water during the reaction or at least until the time to ensure the commencement of steam extraction, since only fully water-enveloped biomass carbonates hydrothermally or c) preheat the biomass.
  • the heat of the water not mixed with the biomass can preferably be used directly or indirectly via a second heat circuit by means of heat exchangers for preheating the biomass.
  • an efficient separation of water and coal takes place after the hydrothermal carbonization without prior relaxation of the mixture to ambient pressure.
  • a portion of the water can then be circulated at high temperature and pressure and mixed with the biomass prior to the start of the reaction or during the reaction.
  • the control of the internal temperature of a HTC reactor by the pressure-controlled or temperature-controlled removal of water vapor via e.g. one or more valves claimed.
  • the pressure is adjusted in the reactor so that the boiling point of water corresponds to the desired internal reactor temperature.
  • the liberated during the reaction heat is thus expended to evaporate water and removed in the form of water vapor from the reactor.
  • the valve or valves will preferably be mounted on top of the reactor. If the steam can not be used immediately after removal, it can be temporarily stored in a corresponding device.
  • claim 2 is claimed as a preferred process variant, such as the steam after removal for preheating the biomass in the preheater and / or Temperature is introduced into the post-curing.
  • the steam must be compressed.
  • a pressure reduction eg cellular wheel or duck sluice
  • a reduction in pressure between the preheater and the reactor can be particularly useful if a higher temperature is required to initiate the reaction for a short period of time than for its continuation.
  • the introduction of the steam can preferably be realized via one or more valves, which - controlled by one or more temperature measurement in the preheater or follower - open when the desired temperature is not reached and allow the steam to flow in and close again as soon as the desired temperature is reached.
  • the one or more valves are preferably mounted at the bottom of the preheater or follower.
  • the pressure in the preheater and post-processor should be selected so that the water vapor condenses and releases its heat to the biomass.
  • the residence time of the biomass in the preheater is to be chosen so that the reaction is initiated even after the promotion in the reactor still continues to run independently.
  • claim 3 is claimed as a preferred variant of the method, as the water vapor can be introduced without additional compression in the preheater and / or post-conditioner.
  • an increase in pressure for example by an extruder screw or a pump
  • the pressure in the preheater is adjusted so that the boiling point of water above the starting temperature of the reaction of about 180 - 230 0 C.
  • the steam introduced by, for example, one or more valves condenses and releases its heat to the biomass.
  • the one or more valves can be controlled for example via one or more temperature measurement in the preheater. Open the valve (s) when the desired temperature is not reached and let steam flow in and close again when the desired temperature is reached.
  • a pressure reduction can be realized between reactor and post-processor, for example by means of a throttle or a pressure lock. The pressure in the post-processor is adjusted so that the boiling point of water is above the temperature to be maintained. The introduced steam condenses and releases its heat to the biomass.
  • the one or more valves can be controlled via a temperature measurement in the post-processor. Open the valve (s) when the desired temperature is not reached and let steam flow in and close again when the desired temperature is reached.
  • the one or more valves are preferably mounted at the bottom of the preheater or follower. Preferably, the residence time of the biomass in the preheater is to be chosen so that the reaction is initiated even after the promotion in the reactor still continues to run independently.
  • Claim 4 claims as a preferred process variant that the abovementioned process can be used for a continuous, discontinuous or a combination of continuous and discontinuous operation of an HTC plant.
  • the preheating of the biomass can be carried out continuously, while the reaction and / or the post-treatment take place in a batch reactor.
  • the preheating discontinuous and the reaction and / or the post-treatment can be carried out continuously.
  • the method can be used in all possible ways Find combinations of continuous and discontinuous process control.
  • Claim 5 claims, as a preferred variant of the method, that the abovementioned method can also be used for a plurality of systems which are operated in parallel. If several continuous systems are operated in parallel, the extracted steam can be fed to a central steam rail and then withdrawn from there for preheating and post-processing for the same system or the other systems operated in parallel. If several discontinuous plants are operated in parallel and asynchronously undergo the operating states preheating, reaction and post-treatment, the steam withdrawn from the reactor of one or more HTC plants may be fed to preferably a central steam rail and for preheating or post-processing in one or more of the other HTCs Plants are used.
  • Claim 6 claims, as an independent process or as a preferred process variant, that the separation of coal and water after the hydrothermal carbonization does not take place after the mixture has been relieved to ambient pressure, but immediately after the completion of the hydrothermal carbonization. Since the product mixture is at a pressure above the ambient pressure and thus the boiling point is above the normal boiling point of water, the separation of coal and liquid water at a temperature of about 100 0 C can take place. Since the viscosity, density and surface tension of the water decreases with increasing temperature, this also reduces the effort required for the separation. Thus, the advantages of mechanical-thermal dewatering can be used. The energy required for heating is reduced or not needed because the product mixture is available at a high temperature and under pressure following hydrothermal carbonization.
  • separation of water and coal prior to relaxation entails the following advantages:
  • the separated coal can be further dried by flash flash evaporation of part of the water not separated during the separation, resulting in subsequent expansion, and subsequently has a lower humidity than when first flash evaporation and then mechanical separation.
  • the separated water is still available at high temperature and high pressure in liquid form, so that the heat for example by means of heat exchanger back into the HTC system eg for use in a first stage of preheating the biomass coupled by heat exchangers or externally as Use process heat
  • claim 7 is claimed as a preferred process variant that the water separated from the coal completely or partially recirculated and the biomass is mixed before the reaction to, for example, the a) heat capacity of the reactor contents to increase, b) a complete enclosure of the biomass with water during the entire reaction or at least until the start of steam extraction or c) to use the heat of the water of reaction to preheat the biomass.
  • This can in particular bring great efficiency advantages if the separation of water and coal after the reaction and before the relaxation of the mixture to ambient pressure and thus the water is available at high temperatures.
  • the water can then be introduced directly into the reactor or preheater, for example with a pump. The introduction of the water is ideally carried out before the preheating by introducing water vapor.
  • Claim 8 is claimed as a preferred variant of the method that of the coal separated water is completely or partially circulated and the biomass is added during the reaction to, for example, a) increase the heat capacity of the reactor contents, b) a complete enclosure of the biomass with water throughout the reaction or at least until the time of C) to use the heat of the water of reaction to preheat the biomass.
  • This can in particular bring great efficiency advantages if the separation of water and coal after the reaction and before the relaxation of the mixture to ambient pressure and thus the water is available at high temperatures.
  • the water can then be introduced directly into the reactor or preheater, for example with a pump.
  • claim 9 is claimed as a preferred process variant that the heat capacity of the reactor contents, for example by the addition of fresh water or circulating water of reaction is increased so far that the heat of reaction by temporarily increasing the temperature of the reactor contents in the reactor can be cached until they actually can be used.
  • an optimization of the added amount of water as a function of the cost of additional heat required to preheat the reaction mixture and the benefit of the better control of the withdrawal time is made.
  • Claim 10 is claimed as a preferred process variant that the removal of the heat of reaction from the reactor by steam extraction and thus the reactor cooling is delayed until the heat actually preheating the biomass, for temperature maintenance after completion of the exothermic reaction, for post-processing of the products or can be used elsewhere or would be exceeded by a further delay of heat removal, the maximum allowable internal reactor temperature.
  • a control is provided, the dis heat dissipation if necessary but in any case triggers when would be affected by a further increase in temperature of the reaction mixture Reakiionsabiauf.
  • This intermediate storage of the heat of reaction by the heating of the entire reactor contents may be necessary, for example when using the decoupled from a reactor heat for preheating or post-processing of the biomass in another reactor.
  • the biomass is mixed so much water before the beginning of the hydrothermal carbonization that it is completely enclosed by water throughout the Karbonmaschinesvones or at least until the beginning of the steam extraction. Since the hydrothermal carbonization - at least in the first phase - can not be done in a steam atmosphere, this admixture is always required if the biomass does not bring enough self-moisture. For this purpose, for example, the separated from the coal water can be used. The admixture can take place, for example, in the preheater or immediately before the preheater or in the reactor.
  • Claim 12 claims as an independent process or as a preferred process variant that the biomass, if a complete enclosure with liquid water prior to the start of the reaction is not appropriate, it is still preheated and moved to reaction temperature and thus repeatedly brought into contact with liquid water until, for example, the reaction is initiated to such an extent that it continues to run in a steam atmosphere, or the reaction is completely completed or the reaction is partially completed. This may be important, for example, when it is desired to minimize the water demand of an HTC unit or to minimize the water content during the reaction to minimize the expense of post-reaction separation.
  • the movement of the biomass can be done, for example, in the preheater, in which a corresponding listed agitator or a rotating drum is installed.
  • the biomass is heated in the preheater, for example by the injection of steam to the reaction temperature and continuously and discontinuously circulated.
  • a minimum quantity of it must be brought either together with the biomass or separately into the preheater.
  • Claim 13 is claimed as a preferred variant of the method that the water separated from the coal can be evaporated by the use of the heat released in the HTC system and thus processed into liquid fertilizer.
  • claim 14 is claimed as a preferred variant of the method that the removal of the inert gases (CO 2 , CH 4 and others), which are released during the warming of the biomass and during the reaction takes place either in the preheater or between preheater and reactor in, for example, a degassing.
  • the inert gases CO 2 , CH 4 and others
  • the inert gases CO 2 , CH 4 and others
  • Claim 15 a device for the hydrothermal carbonization of biomass is claimed, which is characterized in that for controlling the internal reactor temperature, a pressure-controlled valve is provided, which periodically or continuously deducts water vapor from the reactor and thereby adjusts the internal pressure so that the boiling temperature of the water in the reactor matches the desired internal reactor temperature.
  • a device for the hydrothermal carbonization of biomass is claimed, which is characterized in that this valve can be controlled via a temperature measurement in the reactor and periodically or continuously draws steam at the desired internal reactor temperature is exceeded.
  • Fig. 1 shows a device variant for implementing the above-described method for steam extraction and its reintroduction for a continuous process control.
  • Fig. 2 shows a device variant for implementing the above-mentioned method for steam extraction and its reintroduction for a continuous process control.
  • Fig. 3 shows a device variant for implementing the above-described method for steam extraction and its reintroduction for a discontinuous process.
  • Fig. 4 shows a device for controlling the reactor temperature over the reactor internal pressure.
  • Fig. 5 shows a device for controlling the reactor temperature over the reactor internal temperature.
  • Fig. 6 shows a device variant for the implementation of the above-explained method for the separation of water and coal immediately after leaving the reactor.
  • Fig. 7 shows a device variant for implementing the above-explained method of recycling the separated water.
  • Fig. 8 shows the algorithm for implementing the above-explained method of controlling the timing of steam extraction.
  • Fig. 9 shows a device variant for implementing the above-explained method of extracting inert gases between the point of introduction of the water vapor and the point of extraction of the water vapor.
  • Fig. 10 shows an apparatus for controlling the extraction of inert gases.
  • a hydrothermal carburization plant for biomass, or HTC plant for short comprises as main components (Fig. 1, Fig. 2) a reactor (4), a preheater (1) and a post-processor (9).
  • the reactor (4) is designed so that it can rule in an internal pressure of the reactor, which is above an ambient pressure.
  • the internal pressure of the preheater (1) and / or the post-processor (9) may be lower than the reactor internal pressure, corresponding to the ambient pressure or above. If the pressures in the preheater (1) and in the post-processor (9) below that of the reactor (4) (Fig.
  • a device for pressure reduction (11) is provided between the preheater (1) and the reactor (4) a Device for increasing the pressure (5) and between the reactor (4) and the post-processor (9) a device for pressure reduction (11) is provided. If the pressure in the preheater (1) is above the pressure of the reactor (4) (FIG. 2), and the pressure of the reactor (4) is above that of the post-processor (9), then it is possible between the preheater (1) and the reactor (FIG. 4) a device for pressure reduction (5) or between the reactor (4) and post-processor (9) a device for pressure reduction (11) is provided. At least one valve (6) is mounted on the reactor (4), via which, for example, water vapor can escape from the interior of the reactor to the outside in its open state, as explained in more detail below.
  • the preheater (1) is filled with biomass (2).
  • the biomass is heated inter alia by the introduction of steam through a valve (3) to the minimum reaction temperature depending on the biomass between 180 0 C and 230 0 C and conveyed into the reactor (4).
  • the means for increasing the pressure (5) is provided to realize an increase in pressure between preheater (1) and reactor (4).
  • steam (7) is withdrawn from the reactor through at least one valve (6) to adjust the internal reactor pressure so that the reactor is cooled by the evaporation of water. The internal pressure is thus selected so that the evaporation temperature of water corresponds to the desired internal reactor temperature.
  • the extracted steam (7) is completely or partially circulated and introduced via a valve (3) back into the preheater (1). Additionally, the steam may be introduced through a valve (10) for use in the post-processor (9). Between reactor (4) and post-processor (9), a device for pressure reduction (11) is provided. In addition, a device (8) for temporary storage of the steam can be provided. By increasing the pressure between preheater (1) and reactor (4), it is possible to supply the steam without compression directly to the preheater (1). Due to the pressure reduction between reactor (4) and post-processor (9), it is possible to supply the vapor (7) without compression directly to the post-processor (9). The product (12) is subsequently removed from the post-processor (9).
  • the pressure in the preheater of an HTC system can still be above the pressure in the reactor (Fig. 2).
  • the biomass (2) is introduced into the preheater (1).
  • the biomass is, inter alia, by the introduction of steam by a valve (3) to the starting temperature of the reaction may, depending on the biomass is between 180 0 C and 230 0 C preheated. It is then introduced into the reactor (4).
  • a device for reducing pressure (5) to achieve a pressure reduction between preheater and reactor.
  • steam (7) is withdrawn via at least one valve (6), thereby adjusting the internal reactor pressure such that the heat of reaction is expended to evaporate the water.
  • the extracted water vapor (7) is completely or partially circulated and compressed by a single or multi-stage compressor (13) and introduced via a valve (3) in the preheater (1). There, the biomass is preheated by the condensation of the introduced water vapor. Additionally, the steam may be introduced through a valve (10) for use in the post-processor (9). Between reactor (4) and post-processor (9), a device for pressure reduction (11) is provided. In addition, a device (8) for temporary storage of the vapor (7) can be provided. Due to the pressure reduction between the reactor (4) and post-processor (9), it is possible to Steam (7) without a compression directly to the post-processor (9) to supply. The product (12) is subsequently removed from the post-processor (9).
  • the biomass (1) in the reaction vessel (2) which serves both as a preheater, reactor and as a post-processor, inter alia, by introducing steam (3) to the minimum reaction temperature heated. Due to the onset of the reaction, an independent further heating of the reactor takes place.
  • steam (5) is withdrawn through at least one valve (4) and thereby the internal reactor pressure is adjusted so that the reactor is cooled by the evaporation of water. The internal pressure is thus selected so that the evaporation temperature of water corresponds to the desired internal reactor temperature.
  • the extracted steam is completely or partially recirculated and used again for preheater.
  • a device (6) for temporarily storing the steam is provided. If several reaction vessels are operated in parallel, steam can be taken or supplied from the storage device for all reaction vessels.
  • the device for controlling the temperature (Fig. 4) of the reactor (1) can be realized by a pressure-controlled valve (2).
  • the opening pressure of the valve is adjusted by a controller so that the boiling point of water corresponds to the desired internal reactor temperature.
  • the valve opens and allows water vapor (3) to escape.
  • the resulting pressure drop in the reactor also lowers the temperature. If the setpoint pressure falls below again, the valve closes.
  • the removal of water vapor can also be carried out continuously, if the removal amount is metered so that the internal pressure of the reactor fluctuates around the setpoint. The released heat of reaction is spent in this way for the evaporation of water and removed from the reactor.
  • the device for controlling the temperature (FIG. 5) of the reactor (1) can also be designed such that the control of the valve (3) takes place via a temperature measurement.
  • the valve control is then correspondingly connected to a temperature sensor for detecting the internal reactor temperature.
  • the valve control causes the valve to open and water vapor (3) is withdrawn until the desired internal reactor temperature has fallen below again.
  • the valve closes again.
  • the removal of water vapor can also be carried out continuously, if the removal amount is metered so that the internal temperature of the reactor fluctuates around the setpoint.
  • the separation of water and coal takes place in a separator (3) into which the reaction mixture (2) after exiting the HTC reactor (1) without prior relaxation to ambient pressure occurs.
  • the separated coal (5) is then expanded in a pressure lock (4) to ambient pressure.
  • the vapor (9) produced during the flash evaporation is removed from the lock.
  • the separated water (8) is guided after exiting the separator (3) by a heat exchanger (6), cooled and via a throttle (alternatively a drive) (7), relaxed to ambient pressure.
  • the separation can for example be inserted between the reactor (4 in Fig. 1 or 2) and the post-processor (9 in Fig. 1 or 2), the separated coal (5) - before or after the expansion in the pressure lock - in the follower (9 in Fig. 1 or 2).
  • the circulation of the water can be realized, for example, as follows
  • the coal and water mixture (4) is removed after completion of the hydrothermal Karbonmaschinesretress without relaxation to ambient pressure from the reactor (3) and introduced into the separator (5).
  • the coal is dehydrated discharged from the separator (6) and relaxed via a pressure lock (7).
  • the vapor (14) produced during the flash evaporation is removed from the pressure lock.
  • the separated water (8) is also removed from the separator (5).
  • a part of this (10) is then introduced by means of a pump (11) via a valve (12) in the preheater (1) (alternatively or additionally, the reactor (3)) and mixed with the incoming there biomass (14).
  • the not circulated water (9) is via a throttle (alternatively a drive) (13) relaxed and discharged from the HTC system.
  • the non-recirculated water can also be recooled as shown in Fig. 6 by a heat exchanger to bring the heat gained elsewhere in the HTC system again or otherwise use.
  • the intermediate storage (FIG. 8) of the heat of reaction in a first reactor by heating the contents of the reactor until it can be used in another reactor is for example as follows: Reactor 1 is preheated (a), the reaction starts after the minimum reaction temperature has been exceeded and heats the reactor contents (b), wherein the cooling by heat extraction, for example via heat exchangers or a steam extraction does not start immediately. In parallel, reactor 2 is emptied and refilled (c).
  • the point of removal of the inert gases is genicit as shown in Fig. 9:
  • the biomass (1) is introduced into the preheater and preheated by the condensation of the introduced through a valve (3) water vapor (8).
  • the water vapor was previously removed from the reactor (5) through a valve (6).
  • the degassing dome (4) is located between the point of introduction and condensation of the water vapor in the preheater and the removal of the water vapor from the reactor.
  • the coal (7) withdrawn from the reactor (5) can, as shown in FIG. 1, continue to be introduced into a post-processor.
  • the device for removing the inert gases can be realized by a pressure- and temperature-controlled valve (5) (Fig. 10). From the temperature measured with the temperature sensor (3), the corresponding boiling pressure of water is determined at suitable intervals using a suitable algorithm. If the pressure measured with the pressure sensor (2) is not only marginally higher, the valve (5) opens and the inert gases (6) can flow out. It only closes again when the pressure recorded with the pressure sensor (2), the boiling pressure of water, which corresponds to the temperature recorded by the temperature sensor (3), has approached sufficiently.

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  • Combustion & Propulsion (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

La présente invention concerne un procédé de conduite de processus dans une installation de carbonisation hydrothermale de biomasse, comprenant la séparation et l'utilisation des produits, ainsi qu'un dispositif correspondant.
PCT/EP2008/003932 2007-05-11 2008-05-09 Procédé et dispositif de carbonisation hydrothermale (htc) de biomasse à l'aide d'une installation htc WO2008138637A2 (fr)

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DE102007022840A DE102007022840A1 (de) 2007-05-11 2007-05-11 Verfahren zur Kühlung und Vorwärmung einer Anlage zur hydrothermalen Carbonisierung von Biomasse
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WO2009095015A1 (fr) * 2008-01-30 2009-08-06 Simon Albert Breitbach Procédé de carbonisation de substances organiques
DE102008028953A1 (de) * 2008-06-18 2009-12-24 Hydrocarb Gmbh & Co. Kg Verfahren zur Erzeugung von Kohle aus Pflanzen und Pflanzenresten
EP2166061A1 (fr) 2008-09-18 2010-03-24 Artes Biotechnology GmbH Dispositif et procédé destinés au traitement de biomasse
EP2206688A1 (fr) * 2008-12-16 2010-07-14 Suncoal Industries Gmbh Préparation thermochimique de l'eau de traitement d'une carbonisation hydrothermale
WO2010092040A1 (fr) 2009-02-10 2010-08-19 Csl Carbon Solutions Ltd. Procédé hydrothermal pour la préparation d'un matériau de type charbon à partir d'une biomasse et colonne d'évaporation
WO2010097073A1 (fr) * 2009-02-24 2010-09-02 Hydrocarb Gmbh & Co. Kg Procédé de production de matière première et de fournisseurs d'énergie à partir de végétaux et de débris de végétaux
WO2010133696A3 (fr) * 2009-05-22 2011-01-06 Addlogic Labs Gmbh Dispositif de carbonisation hydrothermale de biomasse
EP2284141A1 (fr) 2009-08-12 2011-02-16 Leibniz-Institut für Agrartechnik Potsdam-Bornim e.V. (ATB) Procédé et dispositif de fabrication de particules de charbon enrichies avec des matières minérales
EP2366757A1 (fr) * 2008-11-17 2011-09-21 Ingelia, S.L. Système de régulation de pression et de température d'au moins un réacteur chimique
EP2388305A3 (fr) * 2010-05-17 2012-01-25 TerraNova Energy GmbH Utilisation thermique de carburants solides
EP2410035A1 (fr) * 2010-07-21 2012-01-25 Revatec GmbH Procédé et dispositif de carbonisation de biomasse à l'aide d'une commande de vapeur
EP2474591A1 (fr) 2011-01-10 2012-07-11 CSL Carbon Solutions Ltd Synthèse de matière humique synthétique par carbonisation hydrothermale
EP2484434A1 (fr) * 2011-02-05 2012-08-08 GRENOL IP GmbH Réacteur de carbonisation hydrothermale fonctionnant en continu
DE102011001108A1 (de) * 2011-03-04 2012-09-06 Ava-Co2 Schweiz Ag Verfahren und Vorrichtung zur hydrothermalen Karbonisirung
WO2013076362A1 (fr) * 2011-11-21 2013-05-30 Kemira Oyj Procédé de traitement de biomasse
EP2612842A1 (fr) 2012-01-05 2013-07-10 CSL Carbon Solutions Ltd Appareil de chauffage de dépôt de biomasse
DE102012002098A1 (de) 2012-02-06 2013-08-08 Eurofoam Deutschland Gmbh Hydrothermale Karbonisierung von Kunststoffmaterial
DE102012019659A1 (de) * 2012-10-08 2014-04-10 Terranova Energy Gmbh Verfahren zur Herstellung von Düngemittel
CN103724056A (zh) * 2014-01-23 2014-04-16 杭州互惠环保科技有限公司 基于水热碳化的生活垃圾清洁增值处理方法
CN103722002A (zh) * 2014-01-23 2014-04-16 杭州互惠环保科技有限公司 基于厌氧消化和水热碳化的生活垃圾综合处理方法
EP2835413A2 (fr) 2013-08-07 2015-02-11 Eurofoam Deutschland GmbH Schaumstoffe Particule d'une matière solide similaire au charbon, utilisations et procédé de fabrication
CN105861003A (zh) * 2016-03-30 2016-08-17 嘉兴职业技术学院 一种生物质预增压水热炭化方法
CN109351297A (zh) * 2018-11-29 2019-02-19 清华大学 一种水热反应系统及其运行方法
CN110499174A (zh) * 2019-09-20 2019-11-26 吉林伸飞环保能源有限公司 一种黄色秸秆炭化器装置
EP3656836A1 (fr) * 2008-11-21 2020-05-27 Antacor Ltd. Procédé et dispositif de fabrication de matériaux ou de combustibles
EP3792225A4 (fr) * 2018-06-14 2021-07-21 Mitsubishi Power, Ltd. Dispositif de traitement hydrothermique, usine de fabrication de biocombustible, procédé de traitement hydrothermique et procédé de fabrication de biocombustible
DE102021129783A1 (de) 2021-11-16 2023-05-17 Gesellschaft zur Förderung von Medizin-, Bio- und Umwelttechnologien e.V. Verfahren zur Produktion von Sorptionsmaterialien aus Gärresten einer Biogasanlage

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Cited By (46)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2009095015A1 (fr) * 2008-01-30 2009-08-06 Simon Albert Breitbach Procédé de carbonisation de substances organiques
DE102008028953A1 (de) * 2008-06-18 2009-12-24 Hydrocarb Gmbh & Co. Kg Verfahren zur Erzeugung von Kohle aus Pflanzen und Pflanzenresten
EP2166061A1 (fr) 2008-09-18 2010-03-24 Artes Biotechnology GmbH Dispositif et procédé destinés au traitement de biomasse
EP2366757B1 (fr) 2008-11-17 2016-02-17 Ingelia, S.L. Système de régulation de pression et de température d'au moins un réacteur chimique pour traiter de la biomasse
EP2366757A4 (fr) * 2008-11-17 2014-06-18 Ingelia S L Système de régulation de pression et de température d'au moins un réacteur chimique
EP2484437A3 (fr) * 2008-11-17 2017-01-18 Ingelia, S.L. Procédé de carbonisation de biomasse hydrothermale et installation pour la mise en oeuvre de ce procédé
EP2366757A1 (fr) * 2008-11-17 2011-09-21 Ingelia, S.L. Système de régulation de pression et de température d'au moins un réacteur chimique
EP3656836A1 (fr) * 2008-11-21 2020-05-27 Antacor Ltd. Procédé et dispositif de fabrication de matériaux ou de combustibles
EP2206688A1 (fr) * 2008-12-16 2010-07-14 Suncoal Industries Gmbh Préparation thermochimique de l'eau de traitement d'une carbonisation hydrothermale
WO2010092040A1 (fr) 2009-02-10 2010-08-19 Csl Carbon Solutions Ltd. Procédé hydrothermal pour la préparation d'un matériau de type charbon à partir d'une biomasse et colonne d'évaporation
DE102009010233A1 (de) * 2009-02-24 2010-11-11 Hydrocarb Gmbh & Co. Kg Verfahren zur Gewinnung von Rohstoff und Energieträgern aus Pflanzen und Pflanzenresten
DE102009010233B4 (de) 2009-02-24 2020-06-10 Revatec Gmbh Verfahren zum Erzeugen von Kohle aus Biomasse
WO2010097073A1 (fr) * 2009-02-24 2010-09-02 Hydrocarb Gmbh & Co. Kg Procédé de production de matière première et de fournisseurs d'énergie à partir de végétaux et de débris de végétaux
WO2010133696A3 (fr) * 2009-05-22 2011-01-06 Addlogic Labs Gmbh Dispositif de carbonisation hydrothermale de biomasse
EP2284141A1 (fr) 2009-08-12 2011-02-16 Leibniz-Institut für Agrartechnik Potsdam-Bornim e.V. (ATB) Procédé et dispositif de fabrication de particules de charbon enrichies avec des matières minérales
WO2011018505A3 (fr) * 2009-08-12 2011-04-07 Leibniz-Institut für Agrartechnik Potsdam-Bornim e.V. Dispositif et procédé pour produire du biogaz et du biocharbon, et pour raffiner du biocharbon
WO2011018505A2 (fr) 2009-08-12 2011-02-17 Leibniz-Institut für Agrartechnik Potsdam-Bornim e.V. Dispositif et procédé pour produire du biogaz et du biocharbon, et pour raffiner du biocharbon
EP2388305A3 (fr) * 2010-05-17 2012-01-25 TerraNova Energy GmbH Utilisation thermique de carburants solides
EP2410035A1 (fr) * 2010-07-21 2012-01-25 Revatec GmbH Procédé et dispositif de carbonisation de biomasse à l'aide d'une commande de vapeur
EP2474591A1 (fr) 2011-01-10 2012-07-11 CSL Carbon Solutions Ltd Synthèse de matière humique synthétique par carbonisation hydrothermale
WO2012095408A1 (fr) 2011-01-10 2012-07-19 Csl Carbon Solutions Ltd. Synthèse d'une matière humique artificielle par carbonisation hydrothermale
EP2484434A1 (fr) * 2011-02-05 2012-08-08 GRENOL IP GmbH Réacteur de carbonisation hydrothermale fonctionnant en continu
DE202011110246U1 (de) 2011-03-04 2013-04-25 Ava-Co2 Schweiz Ag Vorrichtung zur hydrothermalen Karbonisierung
DE102011001108A8 (de) * 2011-03-04 2012-11-08 Ava-Co2 Schweiz Ag Verfahren und Vorrichtung zur hydrothermalen Karbonisierung
WO2012119875A1 (fr) 2011-03-04 2012-09-13 Ava-Co2 Schweiz Ag Procédé et dispositif de carbonisation hydrothermique
DE102011001108A1 (de) * 2011-03-04 2012-09-06 Ava-Co2 Schweiz Ag Verfahren und Vorrichtung zur hydrothermalen Karbonisirung
DE102011001108B4 (de) * 2011-03-04 2015-03-12 Ava-Co2 Schweiz Ag Verfahren und Vorrichtung zur hydrothermalen Karbonisierung
WO2013076362A1 (fr) * 2011-11-21 2013-05-30 Kemira Oyj Procédé de traitement de biomasse
EP2612842A1 (fr) 2012-01-05 2013-07-10 CSL Carbon Solutions Ltd Appareil de chauffage de dépôt de biomasse
EP2615068A1 (fr) 2012-01-05 2013-07-17 CSL Carbon Solutions Ltd Appareil et procédé de préparation continue de dépôt de biomasse désintégré
WO2013117600A1 (fr) 2012-02-06 2013-08-15 Eurofoam Deutschland Gmbh Carbonisation hydrothermale de matière plastique
DE102012002098A1 (de) 2012-02-06 2013-08-08 Eurofoam Deutschland Gmbh Hydrothermale Karbonisierung von Kunststoffmaterial
DE102012019659A1 (de) * 2012-10-08 2014-04-10 Terranova Energy Gmbh Verfahren zur Herstellung von Düngemittel
EP2716619A3 (fr) * 2012-10-08 2017-11-29 TerraNova Energy GmbH Procédé pour la production de fertilisant humique par carbonisation hydrotermale des biomasses
EP2835413A2 (fr) 2013-08-07 2015-02-11 Eurofoam Deutschland GmbH Schaumstoffe Particule d'une matière solide similaire au charbon, utilisations et procédé de fabrication
CN103724056B (zh) * 2014-01-23 2016-03-09 杭州互惠环保科技有限公司 基于水热碳化的生活垃圾清洁增值处理方法
CN103722002A (zh) * 2014-01-23 2014-04-16 杭州互惠环保科技有限公司 基于厌氧消化和水热碳化的生活垃圾综合处理方法
CN103724056A (zh) * 2014-01-23 2014-04-16 杭州互惠环保科技有限公司 基于水热碳化的生活垃圾清洁增值处理方法
CN105861003A (zh) * 2016-03-30 2016-08-17 嘉兴职业技术学院 一种生物质预增压水热炭化方法
CN105861003B (zh) * 2016-03-30 2018-07-10 嘉兴职业技术学院 一种生物质预增压水热炭化方法
EP3792225A4 (fr) * 2018-06-14 2021-07-21 Mitsubishi Power, Ltd. Dispositif de traitement hydrothermique, usine de fabrication de biocombustible, procédé de traitement hydrothermique et procédé de fabrication de biocombustible
US11236001B2 (en) 2018-06-14 2022-02-01 Mitsubishi Power, Ltd. Hydrothermal treatment device, biomass fuel manufacturing plant, hydrothermal treatment method, and biomass fuel manufacturing method
CN109351297A (zh) * 2018-11-29 2019-02-19 清华大学 一种水热反应系统及其运行方法
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
CN110499174A (zh) * 2019-09-20 2019-11-26 吉林伸飞环保能源有限公司 一种黄色秸秆炭化器装置
DE102021129783A1 (de) 2021-11-16 2023-05-17 Gesellschaft zur Förderung von Medizin-, Bio- und Umwelttechnologien e.V. Verfahren zur Produktion von Sorptionsmaterialien aus Gärresten einer Biogasanlage

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