EP4587534A1 - Processus en une étape et dispositif de production d'huile de pyrolyse reformée et de gaz de pyrolyse riche en hydrogène - Google Patents

Processus en une étape et dispositif de production d'huile de pyrolyse reformée et de gaz de pyrolyse riche en hydrogène

Info

Publication number
EP4587534A1
EP4587534A1 EP23771835.8A EP23771835A EP4587534A1 EP 4587534 A1 EP4587534 A1 EP 4587534A1 EP 23771835 A EP23771835 A EP 23771835A EP 4587534 A1 EP4587534 A1 EP 4587534A1
Authority
EP
European Patent Office
Prior art keywords
pyrolysis
reactor
starting material
reaction space
temperature level
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.)
Pending
Application number
EP23771835.8A
Other languages
German (de)
English (en)
Inventor
Simon Meidenbauer
Andreas Apfelbacher
Robert Daschner
Johannes Neidel
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.)
Fraunhofer Gesellschaft zur Foerderung der Angewandten Forschung eV
Original Assignee
Fraunhofer Gesellschaft zur Foerderung der Angewandten Forschung eV
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 Fraunhofer Gesellschaft zur Foerderung der Angewandten Forschung eV filed Critical Fraunhofer Gesellschaft zur Foerderung der Angewandten Forschung eV
Publication of EP4587534A1 publication Critical patent/EP4587534A1/fr
Pending legal-status Critical Current

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Classifications

    • 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
    • C10B3/00—Coke ovens with vertical chambers
    • 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
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/10—Treatment of sludge; Devices therefor by pyrolysis
    • 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
    • C10B1/04—Vertical 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
    • C10B31/00—Charging devices
    • C10B31/02—Charging devices for charging vertically
    • 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
    • C10B33/00—Discharging devices; Coke guides
    • C10B33/02—Extracting coke with built-in devices, e.g. gears, screws
    • 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
    • C10B47/02—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with stationary charge
    • C10B47/06—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with stationary charge in 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
    • C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
    • C10B47/20—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge according to the moving bed type
    • 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
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
    • C10B49/06—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated according to the moving bed type
    • 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
    • C10B51/00—Destructive distillation of solid carbonaceous materials by combined direct and indirect heating
    • 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
    • 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
    • C10B57/02—Multi-step carbonising or coking processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
    • C10C5/00—Production of pyroligneous acid distillation of wood, dry distillation of organic waste
    • 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/20—Nature of the water, waste water, sewage or sludge to be treated from animal husbandry
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/22—Nature of the water, waste water, sewage or sludge to be treated from the processing of animals, e.g. poultry, fish, or parts thereof
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/26—Nature of the water, waste water, sewage or sludge to be treated from the processing of plants or parts thereof
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/26—Nature of the water, waste water, sewage or sludge to be treated from the processing of plants or parts thereof
    • C02F2103/28—Nature of the water, waste water, sewage or sludge to be treated from the processing of plants or parts thereof from the paper or cellulose industry
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/32—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/32—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters
    • C02F2103/322—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters from vegetable oil production, e.g. olive oil production
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/32—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters
    • C02F2103/325—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters from processes relating to the production of wine products
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • 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
    • C10G2300/1003—Waste materials
    • 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
    • C10G2300/1014—Biomass of vegetal origin
    • 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
    • C10G2300/1018—Biomass of animal origin

Definitions

  • the present disclosure of the invention is a significant simplification of the thermocatalytic process according to the prior art.
  • a clear characteristic or distinction between classic pyrolysis oils and the reformed oils according to the application is the significantly higher product quality.
  • the pyrolysis gases according to the application a very high hydrogen content (>20% by weight) and in the case of the oil according to the application, a low polarity, a low acid number and a low amount of oxygen in the oil (CHNO).
  • the residence time of the solid in the downpipe can be regulated using the discharge screw.
  • Pyrolysis of the starting material or biomass now takes place in the downpipe; Coke and pyrolysis vapors are formed. These travel further down the pipe; The bulk material in the pipe is heated, in particular by means of a temperature gradient, to a coke temperature or the highest realized temperature level, which is between 450 and 900 ° C. Since there is hot pyrolysis coke in the lower part of the tube and the pyrolysis vapors are guided on the process side in such a way that they are passed through the hot coke bed, reforming takes place at the same time as pyrolysis in the same tube.
  • the tubular reactors according to the application are very robust against higher pressures. If a lock system is connected upstream or downstream of the tubular reactor on the input and discharge sides, the reactor can be operated in a pressure range of several bar, typically up to 30 bar, in particular up to 10 bar, for example also in a pressure range of more than 1.5 bar up to 5 bar, for example also in a pressure range of more than 2.5 bar. Better product qualities and yields can usually be achieved with higher pressures.
  • the reactor is designed to be pressure-resistant, pressures of 200 bar and more can be achieved, although from an economic point of view it is more advantageous to design the reactor up to 30 bar.
  • the method according to the application could also be carried out at pressures below normal pressure, for example at a pressure of a few mbar; Here too, this is not advantageous from an economic point of view.
  • a higher pressure is an advantage because it can usually significantly reduce the formation of long-chain hydrocarbons (especially tars).
  • Figure 1 shows the schematic representation of a downpipe reactor 1 in the “annular gap” variant.
  • the downpipe reactor 1 is filled with bulk material up to a level L.
  • Three heating devices 1 1 , 12 and 13 arranged vertically one above the other are arranged on the side, of which at least the upper two heating devices 1 1 , 12 serve to adjust the first and second temperature levels.
  • Below the middle heating device 12 (which serves to set the second (i.e. the highest) temperature level in the bulk material) is the outlet 15 for pyrolysis gases and pyrolysis vapors.
  • the outlet 15 is designed here as an annular gap; Pyrolysis gases and pyrolysis vapors can be subsequently processed, for example by condensation, dust separation (in the cyclone) and/or aerosol separation (using an e-filter).
  • the discharge device 18 for the pyrolysis coke is arranged at the lowest end of the reactor; A screw conveyor is used to control the residence time of the solids.
  • a feed device 8 for the starting material is arranged at the upper end of the reactor; This is equipped with a lock so that the reactor input can be sealed gas-tight on the side.
  • the reactor is therefore initially filled with the starting material via the feed device 8 until the desired level L is reached.
  • the uppermost heating device 11 sets the temperature level of at least 300 ° C, and the second temperature level of at least 450 ° C is set by the heating device 12.
  • the second (i.e. the highest) temperature level (regardless of the selected reactor geometry) will have a temperature of at least 550 °C.
  • the reactor can then operate in batch mode or continuously be operated, with starting material being supplied accordingly via the feed device 8.
  • the starting material passes through the reaction space in a vertical direction essentially due to the presence of gravity;
  • the feed can also be controlled via the speed of the discharge via the discharge device 18.
  • Figure 2 shows the schematic representation of a downpipe reactor in the “riser pipe” variant, in which the gas outlet 15, in contrast to Figure 1, does not take place via an annular gap but via a riser pipe. It can be seen here that the lower end of the gas outlet 15 is arranged below the middle heating device 12 and still projects into the area in which the lowest heating device 13 is arranged. The possible position of several temperature sensors is not provided with reference numbers.
  • the lowest heating device 13 here only serves to improve the coal quality of the pyrolysis coke formed, for which a long coal residence time is crucial. Accordingly, it no longer sets a temperature that - as in FIG. 1 - is above the temperature level that is achieved by means of the heating device 12.
  • FIG 3 shows the schematic representation of a downpipe reactor 1 in the “flue gas ducts/lance” variant.
  • a large reactor diameter can be achieved, particularly with this type of reactor.
  • the heating devices are not (or not only) arranged on the outer surface of the reactor but (also) in its interior.
  • the heating devices 11, 12, 13 are designed here as flue gas channels 14, with the flue gas flowing through the channels from bottom to top, so that a temperature gradient can be realized in the reactor.
  • the temperature control takes place in such a way that the flow velocity of the heating gas, in particular flue gas, is selected so that a temperature gradient is formed and the heating gas at the lower end of the flue gas channels 14 has at least the temperature of the second temperature level and at the upper end of the flue gas channels 14 at a maximum the temperature of the first Temperature levels (wherein regardless of the reactor geometries described in this section, the first temperature level is typically at least 50 ° C lower than the second temperature level and usually also at least 100 ° C lower. The difference in temperature levels is usually - as already explained above - more as 100 ° C (in particular up to 300 ° C).
  • a first temperature level is chosen between 350 and 450 ° C and a second temperature level is mentioned, which is chosen between 500 and 700 ° C.
  • Figure 3 also shows a form of training, in which the outlet 15 for pyrolysis gases and pyrolysis vapors is arranged vertically at the bottom in the reactor; Specifically, the pyrolysis gases and pyrolysis vapors are only separated from the pyrolysis coke in the area of the discharge screw 18.
  • the throughput of starting material can be adjusted by timing the screw conveyor.
  • the temperature control is selected so that the first temperature level is reached at the lower end of the upper heating mat and on average the second temperature level is reached at the lower end of the middle heating mat.
  • the reactor is filled so that a volume of up to a level L of just under 1.2 m is filled with bulk material, so that the upper end of the top heating mat approximately corresponds to level L. This means that when sewage sludge granules are used as the starting material, a bulk density of approximately 500 to 550 kg/m 3 is achieved.
  • the bulk material is essentially formed by pyrolysis coke during operation.
  • the pyrolysis gases and pyrolysis vapors generated during the combined pyrolysis/reforming process flow through the coke bed before being fed to the outlet for pyrolysis gases and pyrolysis vapors.
  • the reactor section which is typically arranged in the lower region of the second heating device and in which the highest temperature level is achieved.
  • the pyrolysis vapors can flow through a cyclone for dedusting downstream of the outlet and are then cooled down. Oil and water are then separated from the gas phase.
  • the system can, if necessary, be constantly blanketed with a small amount of nitrogen.
  • test series does not have an upstream pyrolysis reactor;
  • the temperature control via the heating mats is chosen so that a temperature gradient between 250 to 300 °C and 500 to 700 °C is formed (hereinafter these tests are referred to as 1.1 to 1.4).
  • Each sub-test is carried out with a feed quantity of 150 kg of sewage sludge granules, which was purchased from the sewage sludge drying company E&T Aichaberg and had a bulk density of approx. 500 g/l.
  • the dry matter of the sewage sludge granules used had 31% carbon, 4.3% hydrogen, 4.4% total nitrogen, 1.2% sulfur, 18% oxygen and an ash content (at 815 ° C) of 41%; Using mass spectrometry it was possible to determine that about 1 1 -13% transition metals are contained (in each case mass percent is given). The total water content was between 5 and 10 percent by mass. The partial tests can be found in Table 1 below: Table 1
  • Figure 4 shows the mass balances of the product range produced. It can be seen that with (economically less relevant) slow throughput times, significantly more gas and significantly less oil is formed with the method according to the application (1.1 to 1.4) than with faster throughput times (and lower temperatures). However, compared to the TCR tests (2.1 to 2.4), the oil content in the process according to the application is significantly higher.
  • Table 2 shows the parameters of the oil formed.

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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)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

L'invention concerne un processus de production d'huile de pyrolyse, de gaz de pyrolyse et de coke de pyrolyse, dans lequel un matériau de départ, qui comprend sensiblement de la biomasse, est fourni à un réacteur de pyrolyse dans la région supérieure de celui-ci. Le réacteur comprend une chambre de réacteur sensiblement verticale qui est sensiblement tubulaire. Une couche tassée d'un matériau en vrac est présente dans la chambre de réaction, ledit matériau en vrac comprenant le matériau de départ à pyrolyser et, éventuellement, le coke de pyrolyse. Ce matériau en vrac est traité thermiquement dans le réacteur de pyrolyse, le coke de pyrolyse, les gaz de pyrolyse et les vapeurs de pyrolyse étant formés à partir du matériau de départ à pyrolyser, et le matériau en vrac, les gaz de pyrolyse et les vapeurs de pyrolyse étant conduits à travers la chambre de réaction de haut en bas. Le mouvement du matériau en vrac est provoqué sensiblement par la gravité, et le mouvement des gaz de pyrolyse et des vapeurs de pyrolyse est provoqué par la pression de gaz qui s'accumule. Le traitement thermique s'effectue au moins à un premier niveau de température de 300 à 650 °C et ensuite à un second niveau de température, qui est supérieur au premier niveau de température, de 450 à 900 °C.
EP23771835.8A 2022-09-14 2023-09-13 Processus en une étape et dispositif de production d'huile de pyrolyse reformée et de gaz de pyrolyse riche en hydrogène Pending EP4587534A1 (fr)

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