EP3146026A1 - Method for the hydrothermal carbonisation of a biomass and associated device - Google Patents
Method for the hydrothermal carbonisation of a biomass and associated deviceInfo
- Publication number
- EP3146026A1 EP3146026A1 EP15798565.6A EP15798565A EP3146026A1 EP 3146026 A1 EP3146026 A1 EP 3146026A1 EP 15798565 A EP15798565 A EP 15798565A EP 3146026 A1 EP3146026 A1 EP 3146026A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- biomass
- station
- treatment station
- treatment
- heating means
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn
Links
Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B1/00—Retorts
- C10B1/02—Stationary retorts
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/04—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition
- C10B57/06—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition containing additives
-
- 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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/02—Combustion or pyrolysis
-
- 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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/06—Heat exchange, direct or indirect
-
- 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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/10—Recycling of a stream within the process or apparatus to reuse elsewhere therein
-
- 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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/14—Injection, e.g. in a reactor or a fuel stream during fuel production
- C10L2290/141—Injection, e.g. in a reactor or a fuel stream during fuel production of additive or catalyst
-
- 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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/30—Pressing, compressing or compacting
-
- 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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/46—Compressors or pumps
-
- 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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/50—Screws or pistons for moving along solids
-
- 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 the field of thermal and chemical treatment of a biomass such as sludge from a wastewater treatment sector.
- the present invention more particularly relates to a method of hydrothermal carbonization of a biomass and a device for implementing such a method.
- a hydrothermal carbonization process typically consisting in subjecting a biomass to a temperature close to 200 ° C. and at a pressure close to 20 bars.
- EP 2 388 305 A2 describes an installation comprising a treatment path in which a biomass is circulated, this path comprising in particular a heat exchanger and a reactor.
- the heat exchanger is arranged to heat the biomass circulating in the path through a transfer circuit in which circulates a transfer fluid. After having been preheated in this heat exchanger, the biomass is then carbonized in the reactor in which it performs an average residence time of about 4 hours.
- Patent EP 2,388,305 A2 furthermore reports test results according to which the injection of an additive such as glycerine into the biomass makes it possible to significantly reduce the viscosity of this biomass and to significantly promote the rise in temperature of the mixture comprising the biomass and the additive within the reactor.
- the reactor must provide energy to increase the temperature of the biomass
- the residence time of the biomass within the reactor involves stirring the biomass within the reactor to ensure the heat exchange and homogenize the heating
- the temperature gradient between the heating surface of the reactor and the biomass favors the sedimentation of the biomass, leading to the use of a mixer-wiper in order to eliminate the deposition of the biomass on the internal walls of the reactor, the mixer-wiper also involving maintenance costs and also constituting a risky part for the personnel and a part decreasing the reliability of the installation,
- the residence time inherent in heating the biomass in the reactor limits the volume of biomass that the plant can process and requires increasing the volume of the reactor to treat more biomass
- the rise in temperature of the biomass within the heat exchanger is limited by the relatively high viscosity of the biomass entering the installation; as an indication, a dewatered sludge is at least ten times more viscous than water,
- the thermal characteristics of a sludge-type biomass involve significant injection pump power and therefore a significant cost of electrical energy.
- the present invention is intended in particular to overcome all or part of these disadvantages by proposing a method for heating a biomass, as well as a device for implementing such a method, optimizing the heat exchange and exploiting the thermal energy produced by the implementation of such a method or the operation of such a device.
- the present invention provides a method for heating a moving biomass in an industrial process path having an inlet for the incoming biomass, a heating means and a treatment station, a fraction of the biomass heated by means of heating being returned by a return branch to a mixing station upstream of the heating means to constitute therewith the biomass entering a mixture having a temperature greater than the temperature of the incoming biomass, the heated biomass fraction being taken at an outlet of the treatment station.
- Such a method makes it possible to reduce the viscosity of the biomass upstream of the heating means compared with a method that does not carry out such a return. This results in a reduction in the pressure drop in the path and an improvement in the heat exchange gain at the heating means. This results in a greater increase in temperature of the biomass.
- the biomass is a sewage sludge, preferably dehydrated, and the treatment is a hydrothermal carbonization.
- sewage sludge especially dehydrated, has relatively poor heat exchange coefficients, that is to say, disadvantaging its rise in temperature and involving very large equipment sizes.
- the method according to the invention makes it possible to improve the exchange coefficients of such a sludge.
- the heating means is controlled by means of a control means so that the temperature of the biomass reaches a parameterized temperature before it arrives in the treatment station, the parameterized temperature being between 165.degree. C and 205 ° C, preferably 185 ° C.
- the temperature of the biomass upon arrival at the treatment station is sufficiently high, particularly when the treatment is a hydrothermal carbonization, to avoid having to further increase the temperature of the biomass within the treatment station .
- Another advantage of the elimination of the heating function of the treatment station is that, for a given quantity of biomass to be treated, the volume of the treatment station can be reduced, because the residence time of the biomass, in the station of treatment, associated with the heating function is no longer necessary.
- the biomass is put under pressure between the mixing station and the heating means, and the pressure of the biomass fraction is lowered in the return branch.
- the relaxation of the biomass fraction circulating in the return branch generates vapor that propagates in the incoming biomass in the mixing station and condenses as it migrates by heating the incoming biomass.
- the condensation of the vapor of this fraction of biomass circulating in the return branch is made possible by the fact that the biomass in the mixing station is under the influence of atmospheric pressure, the mixture being pressurized in the flow path. downstream of the mixing station.
- the vibration generated by the trigger prevents the biomass located in the mixing station from arching, promoting mixing.
- the fraction of expanded biomass and the incoming biomass undergo a mechanical mixing operation (for example using a mixer). Such an operation further promotes mixing.
- the flow rate of the biomass fraction returned to the mixing station is adjusted according to the amount of incoming biomass contained in the mixing station.
- the return of biomass fraction is piloted so that this fraction is effectively returned to the mixing station only when incoming biomass is present in the mixing station.
- the biomass is pressurized upstream of the mixing station, and the pressure of the fraction is raised in the return branch.
- This second variant has the advantage of returning the biomass fraction in the path by mixing it with the incoming biomass. pressurizing, avoiding the use of an energy sink to lower the pressure of the fraction in the return branch.
- the pressure of the biomass upstream of the heating means is raised to a value making it possible to heat the mixture to a temperature above 100 ° C. without boiling.
- the pressure at the output of the pressurizing pump is greater than 3 MPa.
- the path further comprises a cooling station downstream of the treatment station, and a transfer fluid is heated in its path between the cooling station and the heating means.
- the transfer fluid is heated to a temperature higher than that of the biomass at the treatment station.
- the heat transferred to the heating means can thus heat the biomass to said parameterized temperature before arriving at the treatment station.
- the same external heat source is used to heat the transfer fluid and a heat transfer fluid ensuring a temperature maintenance of the biomass at the treatment station.
- the external heat source may consist of a boiler burner.
- heat is recovered from the biomass downstream of the treatment station and this recovered heat is transferred to the biomass upstream of the treatment station.
- heat is recovered from the biomass downstream of the treatment station and this recovered heat is transferred to the biomass upstream of the treatment station via a means of heat exchange (direct or indirect). between the biomass leaving the treatment station and the biomass circulating in the path upstream of the treatment station.
- the method comprises a step of injecting an additive into the biomass upstream of the heating means.
- the injected additive may consist of any catalyst capable of decomposing the organic material, for example an acid such as sulfuric acid or a catalyst as described in patent EP 2 388 305 A2.
- Such an injection step also contributes to lowering the viscosity of the biomass and thus promoting its rise in temperature, and also reduces the fouling phenomena in the path.
- the injection step can be performed downstream or within the heating means.
- a part of the biomass is taken from the treatment station by means of a recirculation branch and this part is returned to the treatment station so as to generate a movement of the biomass in the treatment station. the treatment station.
- Such removal and return of biomass part in the treatment station limits the sticking or deposition of biomass in the treatment station, and to overcome any means or operation to limit such bonding or deposit.
- the portion of biomass is sampled at a flow rate of between 5 and 15 times the flow of biomass entering the treatment station.
- the invention also relates to a device for implementing a method according to various combinations of the characteristics which have just been described, this device comprising an industrial treatment path comprising:
- a pressurizing pump arranged to move the biomass in the path
- heating means capable of heating the biomass
- a treatment station capable of maintaining the biomass at substantially an inlet temperature in the station of treatment, the treatment station being installed downstream of the heating means
- a return branch capable of transferring a fraction of biomass from an outlet of the treatment station to a mixing station.
- the device further comprises injection means capable of injecting an additive into the path.
- the heat exchange means comprises:
- a transfer circuit in which circulates a transfer fluid so as to heat the biomass in the heating means by heat exchange between the transfer fluid and the biomass
- means for circulating the transfer fluid preferably a pump, capable of circulating the transfer fluid in the transfer circuit.
- the device further comprises an external heat source arranged to heat the transfer fluid and a coolant flowing in an envelope of the treatment station.
- the return branch comprises a pressure lowering device, preferably a pressure reducer, for example of the diaphragm or pump or valve type, of the biomass circulating in the return branch.
- the biomass enters the treatment station by a lower part and leaves an upper part.
- the device can be arranged so that the biomass enters the treatment station by a lower part and so by an upper part.
- a biomass especially when it consists of sewage sludge, is denser than the surrounding water.
- the solid fraction, surrounded by undissolved organic matter, will therefore tend to have a gravitational effect at a lower altitude compared to the already solubilized fractions and therefore for which the carbonization reactions are in progress or have already taken place.
- the residence time of a fraction of non-carbonized biomass in the treatment station is thus increased, compared to a device that enters the biomass through an upper part and makes it exit through a lower part.
- the relative increase in residence time of the biomass in the treatment station increases the quality of the treatment.
- the device according to the invention further comprises a recirculation branch arranged to withdraw a portion of biomass in the treatment station and to return this portion of biomass in the treatment station.
- the treatment station comprises a partition arranged to convey to the return branch a fraction of liquid biomass.
- the treatment station is mechanically passive, that is to say having no scraper or mixer.
- the treatment station is a hydrothermal carbonization reactor for sewage sludge.
- FIGURE 1 is a schematic view of a hydrothermal carbonization device according to the invention comprising a pressurizing pump between a mixing station and a heating means,
- FIGURE 2 is a schematic view of a hydrothermal carbonization device according to the invention comprising a pressurizing pump upstream of the mixing station,
- FIGURES 3a, 3b and 3c are schematic views of a treatment station comprising:
- FIGURE 4 is a schematic view of a hydrothermal carbonization device according to the invention comprising a direct heat exchange means.
- variants of the invention comprising only a selection of characteristics described, isolated from the other characteristics described (even if this selection is isolated within a sentence including these other characteristics), if this selection of features is sufficient to confer a technical advantage or to differentiate the invention from the state of the prior art.
- This selection comprises at least one characteristic, preferably functional without structural details, or with only a part of the structural details if this part alone is sufficient to confer a technical advantage or to differentiate the invention from the state of the prior art .
- FIGURE 1 illustrates a preferred embodiment of the invention.
- the device according to the invention comprises an industrial treatment path in which biomass circulates.
- Incoming biomass for example dewatered sewage sludge, enters through an inlet 1 in the path where it is introduced into a mixing station 2.
- the mixing station 2 is preferably a closed silo capable of holding a quantity of biomass of several cubic meters, under atmospheric pressure.
- the mixing station 2 preferably comprises a feed pump (not shown) for filling the mixing station 2 with biomass and a feed screw (not shown) arranged to introduce biomass contained in the mixing station 2 to the mixing station 2. in a pipe connecting the mixing station 2 to a heating means 4, this pipework comprising between the mixing station 2 and the heating means 4 a pressurizing pump 3.
- the pressurizing pump 3 makes it possible to circulate the biomass in the path.
- the pressurizing pump 3 is of a type capable of raising the pressure of the biomass at the pump outlet 3 to a value greater than 3 MPa (piston pump, diaphragm pump or other).
- the biomass is conveyed from the pressurizing pump 3 to the heating means 4.
- the heating means 4 is preferably a heat exchanger.
- This heating means 4 makes it possible to heat the biomass by heat exchange between a transfer fluid flowing in a transfer circuit T and the biomass passing through the heating means 4.
- the transfer fluid for example oil
- T3 an external heat source
- this heat source being for example a boiler burner.
- Piping also connects the heating means 4 to a treatment station 5 to which the biomass is conveyed.
- the treatment station 5 is preferably a reactor comprising a chamber capable of receiving biomass and maintaining this biomass at a pressure typically of between 2 and 3 MPa.
- the unique function of the treatment station 5 is to provide a residence time for subjecting the biomass to chemical reactions, typically hydrolysis.
- the treatment station 5 may alternatively consist of a reactor, baffled or not, cased or not, or for example a tube of sufficient length to ensure the required residence time.
- the biomass from the heating means 4 enters the chamber of the treatment station 5 via a lower part 53, that is to say a part of the treatment station 5. whose altitude is substantially the lowest relative to the implantation of the treatment station 5 in the room housing the device.
- a pipework also connects the treatment station 5 to a cooling station 6.
- the biomass (hydrolysed) leaves the chamber of the treatment station 5 through an upper part 54 from which it is conveyed to the cooling station 6.
- the upper part 54 means a portion of the treatment station 5 whose altitude is substantially the highest relative to the implantation of the treatment station 5 in the room housing the device, as opposed to the lower part 53.
- the biomass may also enter the treatment station 5 through an upper portion and exit through a lower portion.
- the biomass may also enter the treatment station 5 by a lower part and be conveyed from this lower part to an upper part of the chamber by a pipe, the biomass may leave the post chamber treatment 5 by a lower part.
- a fraction of biomass contained in the treatment station 5 is transferred to the mixing station 2 by a return branch R.
- This transferred biomass fraction is preferably taken from an outlet 51 of the treatment station 5 arranged so that the fraction of biomass removed preferably contains a liquid portion rather than a solid portion.
- Different means are preferably used to collect such a fraction.
- the chamber comprises a siphoid partition Cl requiring the biomass to change direction before reaching the exit 51 (located at low altitude).
- a partition C1 causes a decrease in the solid portion (represented by arrows in solid line) in the recirculated fraction, the inertia of the solid portion favoring the liquid portion selection phenomenon (represented by dashed arrows) to constitute the biomass fraction arriving at the outlet 51.
- the outlet 51 is located at a medium altitude and the portion selection liquid is carried out using a deflector type partition C2.
- the outlet 51 is situated at a relatively high altitude, naturally favoring the selection of a liquid portion to constitute the fraction of biomass conveyed towards this outlet 51.
- the fraction of biomass flowing in the return branch R is subjected to the action of a pressure lowering device R1 before it arrives in the mixing station 2.
- This pressure lowering device RI is for example a diaphragm type regulator, pump or valve.
- the arrival of the fraction of biomass expanded by the pressure lowering device RI is preferably located above the feed screw.
- the flow rate of the biomass fraction passing through the pressure-reducing device RI is adjusted by any suitable control means C so that this flow rate is non-zero only if the mixing station 2 contains a sufficient quantity of biomass. incoming, for example on a height of 1 to 2 meters.
- the pressure lowering device RI thus relaxes the biomass fraction taken from the treatment station 5, which has the effect of creating a vapor of this biomass fraction, which is propagated in the incoming biomass contained in the mixing station 2 by condensing and warming up this incoming biomass.
- the cooling station 6 is preferably a heat exchanger.
- the cooling station 6 makes it possible to cool the biomass leaving the treatment station 5 by heat exchange between the transfer fluid flowing in the transfer circuit T and the biomass passing through the cooling station 6.
- the transfer circuit T connects the heating means 4 to the cooling station 6. It thus constitutes, with the heating means 4 and the cooling station 6, a means for exchanging heat between the biomass leaving the heating station. treatment 5 and the biomass circulating in the path upstream of the treatment station 5.
- the transfer fluid is circulated in the transfer circuit T by circulation means T1, typically a pump.
- An external heat source T3 heats the transfer fluid at the level of the heat exchanger T2.
- the biomass circulating in the heating means is heated by the transfer fluid and heated from which it takes part of its heat.
- the transfer fluid also recovers a part of the heat of the biomass circulating in the cooling station 6.
- part of the heat of the biomass circulating in the path downstream of the treatment station 5 is transferred to the biomass circulating in a heat recovery unit 4a installed upstream of the heating means. 4b.
- the heat exchange means carries out a direct heat exchange between the biomass leaving the treatment station 5 and the biomass circulating in the path upstream of the treatment station 5, via the heat recovery unit 4a. .
- the chamber of the treatment station 5 is surrounded by a casing 52 in which a coolant is circulated.
- This coolant is heated and maintained at a temperature capable of maintaining the biomass contained in the chamber at its temperature before entering the treatment station 5, that is to say when the biomass was between the means of heating 4 and the treatment station 5, and able to compensate for thermal losses related to the structure of the treatment station 5.
- Heating of the heat transfer fluid is preferably carried out by the same external heat source T3 as that heating the transfer fluid, at the level of the heat exchanger T2.
- the transfer fluid and the heat transfer fluid can thus be a same fluid, for example oil, circulating in a circuitry arranged to heat the transfer fluid (flowing in the circuit T) and the heat transfer fluid (flowing in the casing 52) to the desired temperatures .
- the differential control of the temperature of the transfer fluid and the coolant is carried out by any appropriate means, for example valves (not shown) mounted on said circuitry and a control of the opening and closing of these valves and the heat source T3.
- the device In order to raise the temperature of the biomass in the path of the heating means 4, the device is piloted, for example by the control means C, so that the heat source T 3 raises the transfer fluid to a temperature greater than that of the biomass contained in the treatment station 5, for example at a temperature close to 210 ° C.
- the treatment station 5 preferably comprises a recirculation branch M for circulating the biomass in the chamber.
- biomass is preferably aspirated in the upper portion 54 (the biomass being more liquid) and this biomass is reinjected into the chamber by a lower portion 53.
- the flow rate of this recirculation is dimensioned so that the biomass circulating in the recirculation branch M is taken with a flow rate of between 5 and 15 times the flow of biomass entering the treatment station 5 from the heating means 4.
- Such a recirculation ensures a good homogeneity of the temperature of the biomass contained in the treatment station 5.
- the circulation of this biomass in the recirculation branch M is preferably provided by a diaphragm pump M1, preferably sealed and offset from the treatment station 5.
- a pump M1 thus installed increases the reliability of the device, this pump M1. for example, can be repaired or maintained without involving the device out of service in its entirety.
- an additive is injected into the biomass in the path, preferably upstream of the heating means 4, 4b, by any means injection 7 suitable, in order to further reduce the viscosity of the biomass.
- the surface of the heat exchangers (heating means 4, 4b and / or cooling station 6), the pipe diameters as well as the volume of the treatment station 5 can thus be reduced.
- the pressurizing pump 3b is installed between the inlet 1 and the mixing station 2.
- the lifting pump R2 is installed between the mixing station 2 and the heating means 4.
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Combustion & Propulsion (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Treatment Of Sludge (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
Description
Claims
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP17195045.4A EP3287510B1 (en) | 2014-11-04 | 2015-10-29 | Method for hydrothermal carbonisation of biomass, and related device |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR1460617A FR3027914B1 (en) | 2014-11-04 | 2014-11-04 | METHOD FOR HYDROTHERMAL CARBONIZATION OF BIOMASS, AND DEVICE THEREFOR |
PCT/IB2015/058360 WO2016071808A1 (en) | 2014-11-04 | 2015-10-29 | Method for the hydrothermal carbonisation of a biomass and associated device |
Related Child Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP17195045.4A Division EP3287510B1 (en) | 2014-11-04 | 2015-10-29 | Method for hydrothermal carbonisation of biomass, and related device |
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EP3146026A1 true EP3146026A1 (en) | 2017-03-29 |
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EP15798565.6A Withdrawn EP3146026A1 (en) | 2014-11-04 | 2015-10-29 | Method for the hydrothermal carbonisation of a biomass and associated device |
EP17195045.4A Active EP3287510B1 (en) | 2014-11-04 | 2015-10-29 | Method for hydrothermal carbonisation of biomass, and related device |
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EP17195045.4A Active EP3287510B1 (en) | 2014-11-04 | 2015-10-29 | Method for hydrothermal carbonisation of biomass, and related device |
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US (1) | US10287505B2 (en) |
EP (2) | EP3146026A1 (en) |
CN (1) | CN106536691B (en) |
AU (1) | AU2015341447B2 (en) |
FR (1) | FR3027914B1 (en) |
WO (1) | WO2016071808A1 (en) |
Families Citing this family (10)
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FR3037057B1 (en) * | 2015-06-05 | 2019-06-14 | Degremont | METHOD AND DEVICE FOR HYDROTHERMAL CARBONIZATION WITH OPTIMIZED ENERGY EFFICIENCY |
EP3372657B1 (en) | 2017-03-10 | 2019-09-25 | HTCycle GmbH | Device for performing a hydrothermal carbonisation reaction |
IT201800020320A1 (en) * | 2018-12-20 | 2020-06-20 | Daniele Basso | Plant and process for the transformation of biomass |
CN109628121B (en) * | 2019-01-22 | 2020-07-14 | 华中科技大学 | System and method for graded co-production of energy chemicals and silicon-carbon materials from rice husks |
EP4077588A1 (en) * | 2019-12-20 | 2022-10-26 | Circlia Nordic ApS | Cost efficient integration of hydrothermal liquefaction and wet oxidation wastewater treatment |
KR102237795B1 (en) * | 2021-02-01 | 2021-04-12 | 주식회사 하이퍼솔루션 | The method for treating highly infectious animal carcasses |
KR102237796B1 (en) * | 2021-02-01 | 2021-04-12 | 주식회사 하이퍼솔루션 | The device for treating highly infectious animal carcasses |
KR102302185B1 (en) * | 2021-03-31 | 2021-09-15 | 주식회사 하이퍼솔루션 | The method for manufacturing fuel by hydrothermal carbonization of medical wastes |
KR102302186B1 (en) * | 2021-03-31 | 2021-09-15 | 주식회사 하이퍼솔루션 | The device for manufacturing fuel by hydrothermal carbonization of medical wastes |
WO2024076806A1 (en) * | 2022-10-07 | 2024-04-11 | Battelle Memorial Institute | Hydrothermal liquefaction heat recovery process |
Family Cites Families (10)
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US7909895B2 (en) | 2004-11-10 | 2011-03-22 | Enertech Environmental, Inc. | Slurry dewatering and conversion of biosolids to a renewable fuel |
DE102007056170A1 (en) | 2006-12-28 | 2008-11-06 | Dominik Peus | Substance or fuel for producing energy from biomass, is manufactured from biomass, which has higher carbon portion in comparison to raw material concerning percentaged mass portion of elements |
ES2710176T3 (en) * | 2007-02-08 | 2019-04-23 | Grenol Ip Gmbh | Hydrothermal carbonization of biomass |
CA2685420A1 (en) * | 2007-03-22 | 2008-09-25 | Fraunhofer-Gesellschaft Zur Foerderung Der Angewandten Forschung E.V. | Method for wet-chemical conversion of biomass by hydrothermal carbonisation |
EP2274405A1 (en) * | 2008-04-17 | 2011-01-19 | CSL Carbon Solutions Ltd | Process for converting biomass to coal-like material using hydrothermal carbonisation |
EP2388305A3 (en) | 2010-05-17 | 2012-01-25 | TerraNova Energy GmbH | Thermal exploitation of solid fuels |
FR2982273B1 (en) * | 2011-11-09 | 2014-03-14 | Commissariat Energie Atomique | DRYING AND TORREFACTION REACTOR OF BIOMASS, PREFERABLY LIGNO-CELLULOSIC |
KR101369960B1 (en) * | 2013-10-02 | 2014-03-06 | 신명산업 주식회사 | Manufacturing method for solid fuel using hydrothermal carbonization reaction |
CN103723899B (en) * | 2014-01-23 | 2015-06-17 | 杭州互惠环保科技有限公司 | Sludge comprehensive treatment method based on anaerobic digestion and hydrothermal carbonization |
CN103755124A (en) * | 2014-01-23 | 2014-04-30 | 杭州互惠环保科技有限公司 | Sludge treatment method based on hydrothermal carbonization |
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- 2015-10-29 AU AU2015341447A patent/AU2015341447B2/en active Active
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- 2015-10-29 CN CN201580039403.XA patent/CN106536691B/en active Active
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- 2015-10-29 US US15/318,371 patent/US10287505B2/en active Active
- 2015-10-29 EP EP17195045.4A patent/EP3287510B1/en active Active
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Also Published As
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CN106536691B (en) | 2020-07-14 |
WO2016071808A1 (en) | 2016-05-12 |
FR3027914A1 (en) | 2016-05-06 |
FR3027914B1 (en) | 2018-05-04 |
US10287505B2 (en) | 2019-05-14 |
EP3287510A1 (en) | 2018-02-28 |
CN106536691A (en) | 2017-03-22 |
AU2015341447B2 (en) | 2020-02-27 |
EP3287510B1 (en) | 2019-08-14 |
AU2015341447A1 (en) | 2017-01-19 |
US20170233659A1 (en) | 2017-08-17 |
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