EP2280776A2 - Dispositif, procédé et utilisation d'un réacteur pour produire des matières premières, des combustibles et des carburants à partir de substances organiques - Google Patents

Dispositif, procédé et utilisation d'un réacteur pour produire des matières premières, des combustibles et des carburants à partir de substances organiques

Info

Publication number
EP2280776A2
EP2280776A2 EP09734729A EP09734729A EP2280776A2 EP 2280776 A2 EP2280776 A2 EP 2280776A2 EP 09734729 A EP09734729 A EP 09734729A EP 09734729 A EP09734729 A EP 09734729A EP 2280776 A2 EP2280776 A2 EP 2280776A2
Authority
EP
European Patent Office
Prior art keywords
reactor
solids
pressure
organic substances
supply
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.)
Ceased
Application number
EP09734729A
Other languages
German (de)
English (en)
Inventor
Uwe Berger
Thomas Willner
Walter Vanselow
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Technische Werke Ludwigshafen AG
Original Assignee
Technische Werke Ludwigshafen AG
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Technische Werke Ludwigshafen AG filed Critical Technische Werke Ludwigshafen AG
Publication of EP2280776A2 publication Critical patent/EP2280776A2/fr
Ceased legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
    • B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
    • B01J8/224—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid the particles being subject to a circulatory movement
    • B01J8/226—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid the particles being subject to a circulatory movement internally, i.e. the particles rotate within the vessel
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2455—Stationary reactors without moving elements inside provoking a loop type movement of the reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2455—Stationary reactors without moving elements inside provoking a loop type movement of the reactants
    • B01J19/246—Stationary reactors without moving elements inside provoking a loop type movement of the reactants internally, i.e. the mixture circulating inside the vessel such that the upward stream is separated physically from the downward stream(s)
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2455—Stationary reactors without moving elements inside provoking a loop type movement of the reactants
    • B01J19/2465—Stationary reactors without moving elements inside provoking a loop type movement of the reactants externally, i.e. the mixture leaving the vessel and subsequently re-entering it
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/26—Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
    • B01J8/003—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor in a downward flow
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
    • B01J8/004—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor by means of a nozzle
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
    • B01J8/0045—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor by means of a rotary device in the flow channel
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
    • B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
    • B01J8/224—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid the particles being subject to a circulatory movement
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
    • B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
    • B01J8/224—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid the particles being subject to a circulatory movement
    • B01J8/228—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid the particles being subject to a circulatory movement externally, i.e. the particles leaving the vessel and subsequently re-entering it
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00433—Controlling the temperature using electromagnetic heating
    • B01J2208/00442—Microwaves
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00743—Feeding or discharging of solids
    • B01J2208/00752—Feeding
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00893—Feeding means for the reactants
    • B01J2208/00902—Nozzle-type feeding elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00245—Avoiding undesirable reactions or side-effects
    • B01J2219/00247—Fouling of the reactor or the process equipment
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1011—Biomass
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock

Definitions

  • the invention relates to an apparatus, a method and the use of a reactor for the production of raw materials, fuels and fuels from organic substances.
  • a device with the features of the preamble of claim 1 is known for example from DE 102 15 679 Al.
  • a process for the direct thermochemical conversion of high molecular weight organic substances into high-quality low-molecular-weight organic products, which are present as low-viscosity liquids at room temperature and are combustible is known.
  • organic substances in the form of preferably solid, renewable raw materials and / or residues are converted by direct liquefaction in highly refined liquid hydrocarbons, with the aim to use them chemically and energetically.
  • This known method is particularly suitable for the production of fuels for conventional vehicle engines, i. for the production of gasoline or diesel.
  • the direct liquefaction process disclosed in DE 102 15 679 A1 is a catalytically thermal conversion process in which high molecular weight organic substances are removed by cracking and upgrading reactions, supported by catalysts, in a direct manner, i. Without detouring through gasification, high quality liquid products are produced.
  • stirred reactors which provide good mixing and are suitable for reactive distillation and as stripping gas reactors.
  • stirred reactors have the disadvantage that the moving components arranged in the reactor, ie the stirring elements, lead to sealing problems when the reactor is operating at high temperatures in the printing operation.
  • flow reactors such as tubular reactors, offer the advantage of a simple design without moving components.
  • baffles for example in the form of static mixer or static mixing elements allows a good mixing of the components.
  • tubular reactors are not suitable for reactive distillation or as a stripping gas reactor and optimal residence time control of the molecules to be cracked is not possible.
  • the molecules to be cracked are sometimes too long, sometimes too short in the reaction zone, resulting in a low product oil yield or an excessively high product gas yield.
  • the invention has for its object to provide a device for the production of raw materials, fuels and fuels from organic substances, which allows for a comparatively simple design efficient implementation of organic substances in the highest possible raw materials, fuels and fuels.
  • the invention is also based on the object of specifying a method and the use of a reactor for the production of raw materials, fuels and fuels from organic substances, each in a simple manner an efficient implementation of organic substances in the highest possible raw, Brenn - and allow fuels.
  • this object is achieved with regard to the device by the subject-matter of claim 1, with regard to the method by the subject-matter of claim 26 and with regard to the use by the subject-matter of claim 31.
  • the invention is therefore based on the idea to provide an apparatus for the production of raw materials, fuels and fuels from organic substances comprising a reactor with an organic substance introduction means, a reaction product discharge means and a reaction energy supply means for the conversion of the organic substances in the reaction products.
  • the reactor comprises a device for forming a reactor internal flow circuit.
  • the reactor of the device according to the invention is therefore a flow reactor which is adapted so that a circulated flow is formed in the interior of the reactor without the need for mechanically moving elements.
  • the reactor-internal flow circuit ensures an optimized product-oriented mixing and reaction result without the need for moving components. This means that operation of the reactor at high temperatures and pressures is possible without resulting in sealing problems.
  • the reactor-internal flow circuit leads to an excellent ing mixing of the components, even if they are present in different phases. In particular, a good mixing of up to three phases with the physical states liquid, gaseous and solid is possible.
  • the device according to the invention also permits very rapid heating of the raw materials and auxiliaries added, so that the reactor is particularly suitable, in particular, for the shock heating disclosed in DE 102 15 679 A1.
  • the reactor-internal flow circuit allows both catalytic and non-catalytic as well as hydrogenating and non-hydrogenating conversion reactions. By means of a reactive distillation or stripping gas function, the reactor offers the prerequisites for product-oriented retention time optimization.
  • the device for forming the reactor-internal circuit comprises at least one propulsion jet nozzle, which opens into a housing of the reactor.
  • a drive medium for example a gas or a liquid
  • the propulsion jet nozzle can have at least two nozzle tubes, so that a separate entry of the organic substances and the injection of a drive medium are made possible.
  • the formation of the reactor-internal flow circuit is assisted by the fact that at least one guide tube is arranged in the housing in alignment with the propulsion jet nozzle. This arrangement enables the formation of a double-loop flow circulation, which leads to a particularly good mixing of the components.
  • the reactor comprises a device for forming a reactor-external circuit, wherein at least one circulation line connects two spaced-apart sections of the reactor.
  • the reactor will allow the formation of a reactor-internal and a reactor-external circulation, i. two circuits, allowed.
  • the connection of two spaced-apart sections of the reactor through the circulation line allows a return, for example of the sump oil for doping of the reactor.
  • the circulation line can be connected to the propulsion jet nozzle, in particular with one of the two nozzle tubes, whereby a particularly compact design of the device is achieved.
  • the reactor-external circuit can have a heating device and / or a filter device?).
  • a degassing device may be arranged upstream within the reactor of the discharge device.
  • the introduction device has a pneumatic and / or mechanical means for supplying solids, whereby a particularly efficient supply of the organic substances in both continuous and discontinuous operation is made possible.
  • the pneumatic and / or the mechanical means for solids supply may have a high temperature resistant non-stick coating.
  • the pneumatic means for supplying solid material is associated with the device for forming the reactor-internal circuit, so that the latter fulfills a dual function with regard to the supply of the organic substances as well as with regard to the formation of the reactor-internal circulation.
  • the pneumatic means for supplying solids can be connected to the propulsion jet nozzle, in particular to one of the two nozzle tubes.
  • One way to realize the pneumatic means for supplying solids is to provide at least one pressure-conveying container which is connectable to the reactor, in particular to the propulsion jet nozzle.
  • a continuous supply of solids can be achieved by providing two pressure-conveying containers, which can be operated alternately.
  • the pneumatic means for supplying solids may comprise a transport gas and / or fluidizing gas device, which is / are connectable to the pressure-conveying container or the pressure-conveying containers, whereby the pressure-conveying container can be pressurized, both with an inert gas and with a reaction gas ,
  • the discharge of a solid from the pressure-conveying container can take place with the aid of the transport gas device, or be supported.
  • the fluidizing function by means of the fluidizing gas device prevents bridging of the solid particles and adhesion of the particles to the container wall.
  • a gas-permeable lining of the pressure-conveying container can be arranged at least in the area of a feed opening of the pressure-conveying container for the fluidizing gas device.
  • a supply means of the transport gas device in the region of a discharge opening of the pressure-conveying container is arranged.
  • the supply means may comprise a lance, which projects into the pressure feed container into the region of the discharge opening, so that the transport gas can be blown in a targeted manner in the desired area.
  • the mechanical means for solids supply can be assigned to the device for forming the reactor-external circuit. Since the reactor-external circuit is, in particular, a circulation or recycling of the bottom phase of the reactor, the mechanical feed of the organic substances in this area is particularly advantageous.
  • the mechanical means for solids supply may be upstream or downstream of a pump of the device for forming the reactor external flow circuit in the conveying direction.
  • the mechanical means for supplying solids may be preceded by a mashing device, so that the organic solids can be suspended or dissolved by a suitable organic liquid or optionally also by water before being fed into the reactor.
  • the mechanical means for solids supply may comprise a lock device, by means of which the solids to be introduced into the reactor can be rendered inert. In addition, can be prevented by the lock device, the escape of gases, vapors and liquids from the reactor and optionally a seal against an increased reactor pressure can be achieved.
  • the mechanical means for solids supply may comprise a screw device with a pressure-locking section, which is arranged downstream of a compression section for forming a locking plug.
  • the mechanical means of solids supply comprises a piston device.
  • the piston device has the advantage that it is possible to convey or feed non-mashed solids, thereby promoting rapid heating in the reactor.
  • the piston device may comprise at least one pressure cylinder, in particular two pressure cylinders, whereby, in the latter case, a continuous delivery is achieved.
  • the process according to the invention is based on the idea of introducing the organic substances into a reactor, converting them into reaction products while supplying reaction energy, and discharging the reaction products from the reactor.
  • a flow circuit is formed in the reactor.
  • a drive medium can be introduced under pressure into the reactor. In this case, a single-phase, two-phase and three-phase operation of the reactor is possible.
  • the invention further encompasses the use of a reactor for the production of raw materials, fuels and fuels from organic substances with an introduction device for the organic substances, a discharge device for reaction products and a device for supplying reaction energy for the conversion of the organic substances into the reaction product.
  • ducts wherein the reactor has a device for forming a reactor-internal flow circuit.
  • the reactor used is preferably a loop reactor.
  • FIG. 1 shows a cross section through the reactor of an apparatus for the production of
  • Fig. 2 is a detail view of the propulsion jet nozzle of the reactor according to Rg. 1;
  • FIG 3 shows another embodiment of a reactor for a device for the production of raw materials, fuels and fuels from organic substances.
  • FIG. 4 shows a cross section through a pneumatic solids supply device in a schematic representation
  • 5 shows a combination of two solids supply devices according to FIG. 4;
  • FIG. 6 shows a cross section through a mashing device in schematic form
  • FIG. 7 shows a cross section through a lock device in schematic form
  • 9a, 9b a cross section through a piston device in two different piston positions
  • Fig. 10 shows a cross section through a piston device with two Druckzylindem
  • Fig. 11 is a schematic representation of the bypass flow filtration circuit.
  • Fig. 1 shows in cross section a reactor which is used according to the invention for the production of raw materials, fuels and fuels from organic substances by way of direct liquefaction.
  • a multi-phase mixing reactor namely a loop reactor, is used.
  • the reactor 10 comprises a housing 16 with a vertically arranged cylindrical jacket 16a.
  • an introduction device 11 is provided through which organic substances are conveyed into the reactor 10.
  • a discharge means 12 for reaction products for example volatile hydrocarbon compounds, is arranged, which is connected, for example, to a distillation column (not shown).
  • heating elements are integrated, which form the means 13 for the supply of reaction energy.
  • the heating elements can be designed for thermal or inductive heating or for heating by means of microwaves.
  • the device 13 may additionally comprise means for pressurizing the reactor, so that both a pressureless as well as a pressurized operation of the reactor 10 is possible.
  • the reactor 10 further comprises a device 14 for forming a reactor-internal, free flow circuit with at least one propulsion jet nozzle 15, which opens into the housing 16 in the upper region of the reactor 10.
  • the propulsion jet nozzle 15 is designed as a double-tube nozzle or as a three-substance nozzle and has two concentrically arranged nozzle tubes 17, 18.
  • Fig. 2 is a detail view of the exit region of the propulsion jet nozzle 15 with the two nozzle tubes 17, 18 is shown.
  • the inner tube 17 extends axially beyond the outer tube 18, wherein between the inner tube 17 and the outer tube 18, an annular gap is formed. This means that medium can be transported into the reactor 10 both through the inner tube and through the outer tube.
  • the inner nozzle tube 17 protrudes from the nozzle exit section by 0.4-6 times the nozzle diameter, i. the exit diameter of the outer nozzle tube 18 addition.
  • the ratio of the diameter of the inner nozzle tube 17 to the diameter of the outer nozzle tube 18 in the region of the outlet opening of the propulsion jet nozzle 15 is between 0.4 and 0.9.
  • the inner tube 17 is connected to a, not shown in FIG. 1 solids supply, in particular a pneumatic solids supply.
  • the outer tube 18 is connected to a recirculation line 21, generally to a device 20 for forming a reactor-external circuit.
  • the propulsion jet nozzle 15 is associated with a guide tube 19 and a Strömungsleitrohr, wherein the guide tube 19 and the propulsion jet nozzle 15 are arranged in alignment.
  • the outlet side of the propulsion jet nozzle 15 can protrude into the guide tube, so that in this area the guide tube 19 concentrically surrounds the propulsion jet nozzle 15. Between the lower edge of the guide tube 19 and a housing bottom 42 of the reactor 10, a gap is provided.
  • the guide tube 19 is open at both axial ends and, together with the propulsion jet nozzle 15, forms part of the device 14 for forming the reactor-internal flow circuit.
  • the ratio of the diameter of the outer shell 16a to that of the flow duct 19 is preferably 3: 1 to 5: 1.
  • the device 20 for forming the reactor-external circuit comprises the circulation line 21, which connects two spaced-apart sections 22, 23 of the reactor 10. Specifically, the circulation line 21 connects a portion located in the upper portion of the reactor 10 to the axial upper end of the reactor 10, thereby forming a reactor-external circuit. In this case, the circulation line 21 connects a region of the reaction 1, the circulation line 21 forms the outer nozzle tube 18 of the propulsion jet nozzle 15 Pump 29 is provided which is suitable for conveying solid matter. The feeding of the organic substances can also take place mechanically via the pneumatic solids supply, ie the pneumatic means 14, whereby a suitable mechanical means 15 for supplying solids to the pump 29 in the conveying direction is either upstream or downstream.
  • the mechanical feed of the organic substances into the reactor-external circuit is indicated in FIG. 1 by a dashed arrow, which is arranged upstream of the pump 29 in the conveying direction.
  • the mechanical solids supply may be provided instead of the pneumatic solids supply or in addition to the pneumatic solids supply.
  • the sump oil outlet 43 is spaced from the axial upper end of the reactor 10 to a level above the sump oil vent 43 and a gas collection space 44 is formed between the liquid level 45 and the upper axial end 46 of the reactor.
  • the mouth of the propulsion jet nozzle 15 is arranged in the axial direction below the sump oil outlet 43, but at least arranged so that it is ensured during operation of the reactor 10 that the mouth of the propulsion jet nozzle 15 is below the liquid level 45.
  • the propulsion jet nozzle 15 is arranged so that a liquid level 45 is established, which lies approximately in a 0.4 to 1.5 times the diameter of the Strömungsleitrohrs 19 corresponding height above the upper axial end of the Strömungsleitrohrs 19.
  • the device 20 for forming the reactor-external circuit may be equipped with heating elements 20a and / or a filter device 20b.
  • the filter device 20b is designed as a bypass filtration, which is integrated into the reactor-external circuit.
  • a partial flow is branched off from the reactor-external circuit (main flow) and fed to the filter device.
  • the oil sludge filtered out of the partial flow is discharged from the filter device and disposed of or further processed.
  • the partial flow filtered in the filter device 20b is returned to the reactor-external circuit (main flow).
  • the supply of the filtered partial flow to the main flow takes place on the suction side of the pump 29 of the reactor-external circuit. This means that the filtered partial flow is the unfiltered Main stream is added.
  • the arranged in the reactor external circuit heating elements 20a are arranged in the embodiment of the branch of the unfiltered partial flow to the filter device 20b upstream, but may also be downstream due to the design.
  • the main flow of the reactor-external circuit after the branch of the partial flow is, as described above, fed back to the reactor 10 or the bottom phase of the reactor 10.
  • the bypass filtration is shown in FIG. 11.
  • the reactor 10 according to FIG. 1 ensures an unexpectedly optimal mixing behavior of the three phases gas, liquid and solid with one another.
  • the reactor cycle ensures a product-oriented residence time control with a deduction of the volatile target products and a selective solids discharge from the remaining volatile in the reactor cycle product fraction.
  • the entry of the solid raw materials and auxiliaries takes place via feed systems which are suitable for being fed in as continuously as possible into a reactor system under high overpressure.
  • the solids entry takes place pneumatically together with a reaction gas or an inert carrier gas directly into the optimum Mixing and reaction zone of the reactor.
  • the reactor 10 is preferably designed as a loop mixer with integrated phase separation without mechanically moving elements, which has a reactor-internal and a reactor-external circuit.
  • FIG. 3 Another embodiment of a reactor 10 is shown in FIG.
  • the reactor 10 in FIG. 3 has a similar construction to the reactor 10 according to FIG. 1 and additionally comprises a degassing device 37, specifically a degassing head 37a for improved gas-liquid separation.
  • the degassing head 37a is disposed between the reactor 10 and the volatile hydrocarbon discharge device 12.
  • the degassing head 37a engages over the reactor 10.
  • the discharge device 12 for the reaction products is provided on the degassing head 37a, as is the sump oil removal 43, which connects the degassing head 37a to the circulation line 21.
  • the circulation line 21 is not completely drawn.
  • the arrangement of the circulation line 21, in particular the connection with the propulsion jet nozzle 15, corresponds to the arrangement according to FIG. 1.
  • the degassing head 37a includes a mist eliminator 47 disposed below and upstream of the volatile hydrocarbon discharge manifold 12 and extending across the cross section of the degassing head 37a.
  • the mist eliminator 47 is provided for the retention of aerosols and adapted accordingly.
  • a drip ring 48 is provided which is molded on the outer edge of the upper axial end of the reactor 10.
  • a drain line 49 is provided according to FIG. 3 on the housing bottom 42 of the reactor 10. This emptying line 49 can also be provided in the reactor according to FIG. 1.
  • the reactor 10 according to FIG. 3 is operated in a similar manner as the reactor 10 according to FIG. 1.
  • the invention also includes embodiments in which more than one propulsion jet nozzle 15, for example two, three, four or even more propulsion jet nozzles 15 are provided.
  • eachmaschinemüse a Strömungsleitrohr 19 is associated.
  • a plurality of propulsion jet nozzles 15 may be associated with a flow guide 19, wherein the flow tube 19 is dimensioned correspondingly larger in this case.
  • the entry means 11 is formed as a pneumatic means 24 for solids supply.
  • the pneumatic means 24 according to Fig. 4 is associated with the device 14 for forming the reactor-internal circuit, i. the pneumatic means 24 is connected to the propulsion jet nozzle 15, in particular to the internally arranged nozzle tube 17 of the propulsion jet nozzle 15.
  • the pneumatic means 24 has a pressure-conveying container 26 which can be connected to the reactor 10 or the propulsion jet nozzle 15 via a valve arrangement, for example via an outlet ball valve 50. Instead of the outlet ball valve 50 other types of valves can be used.
  • the pressure-conveying container 26 comprises an upper cylindrical portion 51 and a lower conical portion 52.
  • a supply means 53 for example with a filling ball valve 53a, is provided.
  • the filling with organic substances is indicated by a corresponding arrow in FIG. 4.
  • the feed device 53 is followed by an exhaust pipe 54 through which displaced air can escape.
  • the pressure-conveying container 26 is connected to a compressed gas device, through which a fluidizing gas and a transport gas are supplied.
  • the gas supply device for transport gas 27a comprises a supply means 40, for example in the form of a lance 40a, which opens in the region of the discharge opening 41 of the storage container 26.
  • a further gas supply device 27b for the fluidizing gas (fluidizing gas device) is provided, which is connected to the compressed gas device and has a supply opening 28 which is arranged in the lower conical section 52 of the pressure conveying container 26.
  • the lower conical section 52 is provided with a gas-permeable lining 39, which is arranged at least in the region of the feed opening 28 of the fluidising gas device 27b.
  • the liner 39 thus forms a porous aeration cone that assists in homogeneous fluidization of the solids.
  • the liner 39 further prevents bridging of the shredded solids in the pressure-conveying container 26.
  • the upper cylindrical portion 51 is also coated with a high-temperature-resistant non-stick coating 38.
  • the lining 39 is open in the region of the discharge opening 41.
  • the pressure-conveying container 26 according to FIG. 4 is operated as follows:
  • the filling ball valve 53a With the filling ball valve 53a open and the exhaust ball valve 54a open, the comminuted solids are introduced via a suitable transport device through the filling line 53b into the pressure-conveying container 26. The air displaced thereby escapes via the exhaust pipe 54.
  • the filling ball valve 53a closes and inert gas first flows through the fluidizing gas device 27b into the pressure-conveying container 26.
  • the exhaust ball valve 54a is closed and the pressure-conveying container 26 is brought to operating pressure by the transport gas and / or fluidizing gas device 27a, 27b, optionally with inert gas or reaction gas.
  • the outlet ball valve 50 opens and transport gas is injected through the lance 40a of the transport gas device 27a in the region of the application opening 41.
  • the solid located in the pressure-conveying container 26, together with the reaction gas is transported through the discharge line 50a to the reactor 10 or the propulsion jet nozzle 15.
  • the solid metered out of the pressure conveying container 26 is discharged.
  • Continuous operation of the pneumatic means 24 may be accomplished by interconnecting at least two or more pressure vessels 26, as shown in FIG.
  • the two pressure-conveying container 26 have a common exhaust pipe 54 and a common discharge line 50a.
  • one of the two containers respectively acts as a storage container, while the solids are conveyed via the respective other container. As soon as this container is empty or is approximately empty, it is switched to the other, temporarily filled container.
  • the pressure-conveying container 26 functioning as a storage container thus serves as a temporary storage (buffer container) and at the same time as a pressure lock between the atmospheric pressure and the required delivery or system pressure.
  • the pressure-conveying container 26 or storage container are filled via a suitable external conveyor with the originating from an external storage solids and then acted upon closing the solids supply for inerting and to build up the required system pressure with gas. This is preferably done with process gas, which is branched off from the conveying gas flow. However, the construction of the required system pressure can also be carried out with externally supplied gas.
  • valve-controlled lock and pipe system is opened to the reactor 10 and the solids are introduced into the reactor together with conveying gas or transport gas, which may also contain the reaction gas.
  • conveying gas or transport gas which may also contain the reaction gas.
  • a storage tank for the solids and gas supply in the reactor works (pressure feed tank 26)
  • the other storage tank is refilled with the next solid charge Before refilling the respective storage tank is depressurized.
  • the pneumatic conveying by the technical adaptation made in the exemplary embodiment according to FIG. 5 to elevated pressures of up to 200 bar and temperatures of up to 300 ° C. represents an optimum device for introducing organic solids into swamp phases for the purpose of direct liquefaction the pressure reactor quickly and directly registered in the liquid sump phase, without being compacted.
  • the solids are free from Ballastyzen, such as mashing liquor, so that the solids in the sump phase can be heated very quickly and with the least possible expenditure of energy to reaction temperature in the order of about 300 to 600 0 C.
  • Ballastystoffen such as mashing liquor
  • FIG. 6 An example of a mechanical means 25 for the supply of solids is shown in FIG. 6 by means of a tempering device 30.
  • the mashing device 30 can be coupled directly to the reactor 10 via a pump 30a.
  • the Anmaisch driving 30 may be provided in addition to the mechanical means 25 for solids supply, for example, when the mechanical means 25 is formed as a screw device 32 or as a piston device 35
  • the mashing device 30 comprises a mashing tank 3Oj with a heating jacket 30b and a stirring / mixing unit 30c.
  • the heating jacket 30b has a first connecting piece 3Od for heating medium inlet and a second connecting piece 3Oe for heating medium outlet. About the controlled supply of heating medium, the mash is preheated in the container to the desired temperature.
  • the mash tank also has a third connection piece 3Of for the liquid feed, an opening 30g for the entry of biomass, a fourth connection piece 30h for the withdrawal of the mash, and a fifth connection piece 30i, which is optionally used for withdrawing the mash or for external recycling of the mash can be.
  • Crushed biomass is continuously discharged via a suitable device 30k into the mixing vessel above the opening 30g.
  • the biomass falls on the surface of an already existing mash, suspension or liquid reservoir.
  • the liquid supplied continuously via the third connection piece 3Of causes, with the aid of the stirring mixer 30c, such a movement of the surface that the biomass is suspended.
  • the mash produced can now be withdrawn via the fifth connecting piece 3Oi and pumped by means of the pump 30a to the reactor 10.
  • the apparatus is equipped with a wet comminution unit 301 in order to further homogenize the mash produced and to comminute any coarse pieces present in the biomass.
  • the wet grinding unit 301 automatically sucks through the fourth connecting piece 30h a partial flow of the mash, which is at least twice as large as the sum of the input streams 10 and 12 and homogenizes the mash.
  • a portion of the mash homogenized by the wet comminution aggregate 301 is sucked by the pump 30a and sent to the reactor, another part flows back into the mash tank via the fifth port 3Oi and generates additional turbulence for mixing the biomass through the opening 30g to the container is supplied.
  • the mashing device 30 has the advantage that the direct introduction of comminuted, moderately tempered solids as a slurry or in slurry form into a sump phase heated to the reaction temperature is made possible. There is no compaction of the crushed solids.
  • the mashing device 30 enables the dissolution or digestion of the solids, preferably in the reactor cycle liquid, i. in oil, water, salt or metal melts or any other organic liquid (e.g., a hydrogen carrier) and optionally a better preheat potential.
  • the mashing device 30 the promotion of the mash (as a slurry or dissolved in the liquid) is made possible by means of pumps which are suitable for suspended solids loads.
  • the solids are suspended or dissolved before being fed into the reactor (pressure reactor or else without pressure) by means of a suitable organic or inorganic liquid or optionally also water, preferably with liquid from the reactor circulation.
  • a suitable organic or inorganic liquid or optionally also water preferably with liquid from the reactor circulation.
  • the ratio of solid to liquid is chosen so that a flowable or pumpable medium is formed.
  • the preparation of this suspension or solution is preferably carried out in a pressureless or under slight overpressure container. As a rule, this container is equipped with a suitable stirring and / or mixing device. After preparation of the suspension or solution and optionally a warm-up, the medium is fed via a suitable pumping device into the bottom phase of the reactor (pressure reactor or pressureless).
  • the mashed solids entry fulfills the requirements of direct liquefaction in the raw materials and liquefied liquids mentioned and represents a particularly inexpensive solution because simple pump systems can be used.
  • FIG. 7 shows a lock device 31.
  • the lock device 31 is constructed as follows and operates according to the following functional sequence:
  • a biomass is conveyed by means of a suitable transport device 31b via a filling hopper 31c with open inlet ball valve 31d in a lock 31e. If the lock 31e is filled, the transport device 31b stops and the inlet ball valve 31d closes. Inertisiergas can via an open ball valve 31f in the lock
  • the exhaust ball valve 31g and the lock 31e may be pressurized to system pressure via a gas stratification gas.
  • the glass ball valve 31f and an outlet ball valve 31h close, whereby the solids contained in the lock 31e are discharged into the reactor 10.
  • the outlet ball valve 31h and the exhaust gas Ball valve 31g opens to drain any existing pressure in the lock 31e.
  • the exhaust ball valve 31g opens the intake ball valve 31d again and the filling process starts again.
  • the lock device 31 has the advantage that a direct entry of comminuted and moderately tempered solids in a heated to reaction temperature bottom phase is made possible without Ballastologisscher be included as Anmaischnetkeit, which delay the heating in the bottom phase reactor.
  • the sluice device 31 when introducing the solids into the reactor 10, allows the solids to be inertized (if this is not already possible in an upstream storage device), prevents the escape of gases, vapors and liquids from the reactor and optionally seals against increased or high reactor pressure.
  • the solids inlet and outlet are equipped with suitable shut-off valves, preferably with ball valves.
  • a rotary valve either as a gravity system or in combination with a pneumatic conveyor
  • a gravity-based lock system works in such a way that the outlet shut-off (if necessary pressure-tight) is closed to fill the lock and the inlet shut-off is opened.
  • the inlet fitting possibly pressure-tight
  • the outlet fitting is closed, while the outlet fitting initially remains closed.
  • the lock space is inertize by means of gas or liquid and possibly build up pressure according to the back pressure in the reactor.
  • the outlet fitting is opened and the contents can be entered by gravity or possibly also by a rinsing process in the reactor or possibly a precursor to the reactor.
  • at least two separate lock spaces are used, which are operated alternately to ensure a continuous solids feed.
  • a quasi-continuous feeding is also possible with a lock.
  • the lock system represents a possibility of removing dry comminuted solid particles at room temperature. temperatures up to 300 0 C enough to enter into a liquid sump phase to elevated pressures up to 200 bar or depressurized quickly.
  • the sluice promotion is surprisingly suitable for entry of said dry organic solids in swamp phases for the purpose of direct liquefaction.
  • the solid particles should be introduced into the reactor (pressurized reactor or pressureless) quickly and directly into its liquid sump phase and should be as free as possible of ballast additives such as mashing liquid, so that they are very fast in the sump phase and with the lowest possible energy input to reaction temperature in the order of up to 500 0 C to be heated. This is important for energy-efficient process control and for a high yield of desired liquid product. With slow heating occur increasingly solid charring and Verte mecanics occur.
  • the sluice promotion fulfills the requirements for the raw materials mentioned and, for these cases, represents a solution which is particularly favorable in terms of plant production costs compared to other entry systems in pressure chambers.
  • the dry solid is supplied via a suitable unit (not shown), and further digested by a corresponding construction of the screw flight 32a in the comminution zone 32b.
  • additives, gas for inerting and / or liquids for mashing and preheating of the solid may optionally be added via openings 32d.
  • the screw device 32 may be e.g. be heated by means of electrical heating strips, which are mounted around the tubular body 32f (housing).
  • the pitch of the screw flight 32a changes and the tube body 32f runs conically, so that here a compression of the solid is achieved and thus a plug against the internal pressure of the high pressure vessel or reactor 10 is built up.
  • the grafting zone 33 serves as a pressure barrier against liquids and gases in the reactor. In this zone 33, the solid is not further compressed, but only advanced.
  • a comminuting or deagglomerating device 32e Prior to entry of the compacted solid into the high pressure vessel or reactor 10, a comminuting or deagglomerating device 32e is present. In the present example, cutters 32a are cut on the extended worm shaft 32a, which chop the strand.
  • the screw device 32 carries crushed, moderately tempered solids directly and continuously into the heated to reaction temperature bottom phase.
  • the screw device 32 offers the possibility of heating the solids with or without mash oil, if appropriate or necessary.
  • a solids entry without Ballastosstoffe such as mashing liquid is possible to avoid a delayed heating in Sumpfphasenreak- gate.
  • it is also possible to introduce solids with mashing liquid it being possible to premix the mash fluid and the solids by means of mixing elements installed in the screw conveyor.
  • the screw device 32 draws the solids (with or without mashing liquid) from an upstream storage tank (usually a buffer tank) into the screw conveyor.
  • a suitable feed device eg feed screw
  • the exit of the screw machine can be provided with a comminution device (eg rotating cutting device), which disassembles the compacted material before the entry of the reactor.
  • the screw device 32 is a possibility of crushing solid particles without sealing problems at temperatures up to 300 ° C. in pressure chambers against elevated pressures of up to 200 bar entered.
  • the solids form a plug, which is impermeable even for pressurized hydrogen.
  • This is the screw conveyor surprisingly suitable for entry of said organic solids in sump phases for the purpose of direct liquefaction under hydrogen pressure or depressurized.
  • the solid particles can be introduced into the reactor 10 (pressure reactor or pressureless reactor) quickly and directly into its liquid bottom phase.
  • the solids should in this case be freely ty is ballast auxiliaries such Anmaischflüs- so that they are heated in the liquid phase very rapidly and with little energy as possible to the reaction temperature in the order of up to 500 0 C. This is important for energy-efficient process control and for a high yield of desired liquid product. With slow heating in the reactor occur increasingly solid Verkohlungs- and Verte mecanics employment.
  • the screw conveyor fulfills the necessary requirements for the mentioned raw materials, in particular when fed into pressure chambers, without the need for a complex system technology. In addition, there are no sealing problems associated with high pressure solids delivery and the need to add mash liquor.
  • the mechanical means 25 for solids supply can also be realized in the form of a piston device 35, as shown in Figures 9a, 9b and 10.
  • FIG. 9a illustrates the suction stroke of the piston device 35.
  • the delivery medium is supplied to the piston device 35 via a worm 35a during the backward movement of the working piston 35b and reaches the product space 35d of the pump or piston device 35 via an opened, hydraulically actuated suction valve 35c.
  • FIG. 9b illustrates the working or pressure stroke of the piston device.
  • the suction valve 35c closes and the pressure cylinder 36 pushes the working piston 35b into the product space 35d, whereby the pressure valve 35e opens and pushes the mash into the pipe 35f to the reactor 10.
  • the pressure-side valve rods 35g are not in the flow range. Through this valve arrangement, the full flow cross-section is available during the pressure stroke.
  • FIG. 10 shows by way of example a piston device 35 with 2 pressure cylinders 36 for continuous conveying:
  • the double-piston device for biomass introduction comprises two parallel pressure cylinders 36 and working pistons 35b, which use a common pressure-conveying line 35f to the reactor 10.
  • the piston device 35 allows the direct, discontinuous or continuous entry of comminuted, moderately tempered solids, which are vermänischt with liquid, in a heated to reaction temperature Sumpfhpase. In addition, there is also the possibility of promoting or feeding untoned solids, creating a fast
  • the piston device 35 offers a good possibility of inerting in the pump pressure chamber between the piston and the discharge shut-off. Furthermore, there is a good possibility of preheating the solids or their mash before it is fed into the reactor 10.
  • the filling area of the piston device 35 is filled with solids (with or without liquefied liquid) from an upstream storage tank (usually a buffer tank).
  • a suitable feed device eg feed screw
  • the discharge tube of the piston device is closed by a suitable lock (eg slider or valve) to the reactor.
  • the piston pushes the material into a tube closed on all sides.
  • the tube space closed by the piston and the lock serves to seal against a possibly present reactor pressure and to build up the required system pressure (sealing against atmosphere or lower pressure stage).
  • the solids or their mash can be preheated by means of suitable heating devices and, if appropriate, the supplied solids and their mash can be rendered inert by externally supplied gases (elimination of air and oxygen).
  • the lock opens to the reactor and the piston pushes the material into the bottom area of the reactor.
  • the reactor feed is discontinuous.
  • a continuous reactor feed is possible via a multi-piston system.
  • the drive of the piston device is usually hydraulically, but can also be performed electrically.
  • the piston device 35 represents a possibility for different raw materials (solid biogenic substances such as energy plants, wood, straw, biowaste, plastic waste and other solid organic substances), crushed solid particles with and without liquid components at temperatures up to 300 0 C in pressure chambers against elevated pressures up to 200 bar.
  • the piston promotion is suitable for entry of said dry organic solids in sump phases for the purpose of pressurized or pressureless direct liquefaction.
  • the solid particles are introduced into the reactor (under pressure or without pressure) quickly and directly into its liquid sump phase and are preferably free from ballast auxiliaries such as mash fluid, so that they are very fast in the sump phase and with as little energy as possible on the reaction temperature in the order of up to 600 0 C to be heated. This is important for energy-efficient process control and for a high yield of desired liquid product. With slow heating occur increasingly solid charring and Verte mecanics employment.
  • the above-described mechanical means 25 for solids supply in particular the Anmaisch worn 30, the lock device 31, the screw device 32 and the piston device 35 can be well used for entry of raw materials or residues in a pressure reactor, in connection with the direct liquefaction of high molecular weight organic Substances in low-viscosity fuels and fuels is used.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Wood Science & Technology (AREA)
  • General Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Processing Of Solid Wastes (AREA)
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Abstract

L'invention concerne un dispositif pour la production de matières premières, de combustibles et de carburants à partir de substances organiques. Le dispositif selon l'invention comprend un réacteur (10) qui présente un dispositif d'introduction (11) pour les substances organiques, un dispositif d'évacuation (12) pour les produits réactionnels, ainsi qu'un dispositif (13) servant à l'apport d'énergie réactionnelle pour la transformation des substances organiques en produits réactionnels. L'invention est caractérisée en ce que le réacteur (10) comprend un dispositif (14) pour la réalisation d'un circuit d'écoulement interne au réacteur.
EP09734729A 2008-04-25 2009-04-24 Dispositif, procédé et utilisation d'un réacteur pour produire des matières premières, des combustibles et des carburants à partir de substances organiques Ceased EP2280776A2 (fr)

Applications Claiming Priority (2)

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DE102008021628A DE102008021628A1 (de) 2008-04-25 2008-04-25 Vorrichtung und Verfahren sowie Verwendung eines Reaktors zur Herstellung von Roh,- Brenn- und Kraftstoffen aus organischen Substanzen
PCT/EP2009/003022 WO2009130045A2 (fr) 2008-04-25 2009-04-24 Dispositif, procédé et utilisation d'un réacteur pour produire des matières premières, des combustibles et des carburants à partir de substances organiques

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US (1) US9592485B2 (fr)
EP (1) EP2280776A2 (fr)
BR (1) BRPI0907327A2 (fr)
CA (1) CA2721201C (fr)
DE (1) DE102008021628A1 (fr)
RU (1) RU2474468C2 (fr)
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FR3083526B1 (fr) 2018-07-04 2020-07-31 Crealyst Group Systeme de remplissage perfectionne
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UA102090C2 (ru) 2013-06-10
BRPI0907327A2 (pt) 2016-07-05
US9592485B2 (en) 2017-03-14
CA2721201C (fr) 2014-01-28
CA2721201A1 (fr) 2009-10-29
US20110219670A1 (en) 2011-09-15
RU2010141174A (ru) 2012-05-27
WO2009130045A3 (fr) 2009-12-23
WO2009130045A2 (fr) 2009-10-29
RU2474468C2 (ru) 2013-02-10

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