EP3060632A1 - Procédé et installation de gazéification d'un matériau de départ - Google Patents

Procédé et installation de gazéification d'un matériau de départ

Info

Publication number
EP3060632A1
EP3060632A1 EP14781446.1A EP14781446A EP3060632A1 EP 3060632 A1 EP3060632 A1 EP 3060632A1 EP 14781446 A EP14781446 A EP 14781446A EP 3060632 A1 EP3060632 A1 EP 3060632A1
Authority
EP
European Patent Office
Prior art keywords
endothermic
synthesis gas
endothermic reactor
gas
gasifier
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Withdrawn
Application number
EP14781446.1A
Other languages
German (de)
English (en)
Inventor
Thomas Heidrich
Gerald GAUBE
Jens Buschmann
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.)
Linde GmbH
Original Assignee
Linde GmbH
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 Linde GmbH filed Critical Linde GmbH
Publication of EP3060632A1 publication Critical patent/EP3060632A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • 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
    • C10B27/00—Arrangements for withdrawal of the distillation gases
    • 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
    • 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
    • C10B57/14—Features of low-temperature carbonising processes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/36—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a conical combustion chamber, e.g. "teepee" incinerators
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/094—Char
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0943—Coke
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/40—Gasification
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2202/00—Combustion
    • F23G2202/10—Combustion in two or more stages
    • F23G2202/101—Combustion in two or more stages with controlled oxidant supply
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2202/00—Combustion
    • F23G2202/10—Combustion in two or more stages
    • F23G2202/103—Combustion in two or more stages in separate chambers
    • 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

Definitions

  • the present invention relates to a method and a plant for the at least partial gasification of solid, organic feedstock, in particular of biomass, with a low-temperature gasifier and a high-temperature gasifier.
  • Processes for the production of synthesis gas from solid organic feedstock also referred to for short as gasification processes, are known.
  • coal or biomass are used as starting material for such processes.
  • biomass gasification processes for example, used wood and forestry wood or so-called energy wood, but also agricultural residues such as straw or chaff are used.
  • synthetic biofuel can be obtained in its
  • Biomass by partial gasification with a gasification agent at temperatures between about 300 ° C and 600 ° C to coke (so-called in the case of biomass
  • Smoldering Registration referred to as "smoldering". Smoldering is known to be characterized by a stoichiometric oxygen supply and thus an incomplete
  • the carbonization gas is then transferred to a combustion chamber of the
  • High-temperature gasifier and transferred there with an oxygen-containing gas for example with more or less pure oxygen, but also with air and / or oxygen-containing exhaust gases, e.g. from gas turbines or internal combustion engines, partially oxidized.
  • an oxygen-containing gas for example with more or less pure oxygen, but also with air and / or oxygen-containing exhaust gases, e.g. from gas turbines or internal combustion engines, partially oxidized.
  • This oxidation released heat causes a temperature increase to 1200 ° C to 2000 ° C, for example 1400 ° C.
  • aromatics, tars and oxo compounds contained in the carbonization gas are completely decomposed.
  • This forms a synthesis gas which consists essentially only of carbon monoxide, hydrogen, carbon dioxide and water vapor.
  • the synthesis gas can also be referred to as (synthesis) raw gas at this point.
  • the synthesis gas thus produced is brought into contact with coke from the low-temperature gasifier, for example in a quench unit integrated in the high-temperature gasifier or in a quench unit connected downstream of it.
  • the coke may be previously treated separately (e.g., by grinding and sifting) and then introduced into the quench unit.
  • the latter is cooled to about 900 ° C. This causes partial conversion of the carbon dioxide to carbon monoxide.
  • the carbon monoxide-rich synthesis gas thus produced can then be further conditioned.
  • the conditioning includes, for example, another
  • High temperature carburetor by partial oxidation and then in an endothermic reactor or carburetor, which may be formed as part of the high-temperature gasifier, converted by partial oxidation and subsequent partial reduction to a synthesis gas. According to the invention can be ensured in a simple manner that in the synthesis gas predominantly on the pyrolysis coke
  • inventively provided side fins can be realized in a structurally simple manner in an endothermic carburetor at a desired height or desired different heights.
  • the invention utilizes that, for example, unwanted (inert) sand particles have an average particle size (particle diameter).
  • the flow velocity of the synthesis gas flowing upward in the endothermic gasifier decreases due to the conical expansion of the carburetor upwards.
  • the (upward) force acting on the foreign particles by the flow is relatively large and exceeds the weight of the particles.
  • these two forces balance out, so that there is an increased concentration of these undesirable particles at this altitude.
  • a side trigger is provided at this height.
  • the at least one side discharge is in operative connection with a vacuum pump, in particular a jet pump.
  • Vacuum pumps unwanted foreign substances can be easily removed from the endothermic carburetor.
  • FIG. 1 shows a plant which is suitable for carrying out a method according to the invention
  • Figure 2 shows a preferred embodiment of a part of an inventive
  • the plant 10 comprises a low temperature carburetor 1 and a
  • a feedstock A for example
  • oxygen can be fed via a line 11.
  • the low temperature carburetor 1 is for fuming the solid organic
  • Feedstock A set up.
  • Via a line 12 can be discharged from the low temperature carburetor 1, a carbonization B and transferred to the high temperature carburetor 2.
  • Hochtemperaturvergaser 2 is formed in two parts. It comprises an oxidation unit 21 and an endothermic reactor (quench unit) 22.
  • the carbonization gas B is partially oxidized with a supplied oxygen-containing gas, resulting in temperatures of, for example, 1400 ° C. to 2000 ° C., as explained.
  • a synthesis gas is obtained, which is designated C.
  • the synthesis gas C is transferred into the endothermic reactor 22.
  • ground coke especially pyrolysis from the
  • Low temperature carburetor 1 A line via which pyrolysis coke is introduced into the endothermic reactor is designated by 23.
  • the gas temperature cools down to approximately 900 ° C. in a short time, at least partial reduction occurs.
  • the resulting gas mixture D which is still referred to as (now carbon monoxide rich) synthesis gas is fed to a cooler 3 and cooled there, for example, to a temperature of 600 ° C.
  • the synthesis gas D can then be dedusted in a cyclone 4.
  • the dedusted synthesis gas E in the context of this application also referred to as "gas mixture derived from the synthesis gas", now has a temperature of, for example, 500 ° C and can in another Cooler 6 are cooled. It can then be supplied, for example, to a carbon dioxide separation device 7.
  • Gas mixture are compacted for example in a compressor 8.
  • the system 10 expediently a pressure regulator 19 with not shown on.
  • the endothermic reactor (quench unit) 22 has an upwardly conically widening shape, as indicated in FIG. 1 and shown in detail in FIG. This endothermic reactor will now be explained in more detail with reference to FIG. It should be noted that the details discussed here can also be implemented in the system according to FIG.
  • the syngas stream denoted by C in FIG. 1 is moved upwards by 90 degrees, for example in a deflection chamber, not shown. redirected to the vertical.
  • the synthesis gas thus flows substantially vertically upwards through the conical endothermic carburetor 22 which widens conically upwards.
  • the ground coke used for the reduction from the low-temperature gasifier 1 is, for example, in the lower region 22a of the endothermic reactor 22 in operative connection with the conduit 23, for example Screw conveyor (symbolically represented by arrow 23a) introduced.
  • This pyrolysis coke reacts in the manner described with the synthesis gas C, wherein the particle size of the pyrolysis coke particles with
  • undesirable foreign particles such as grains of sand, which are predominantly introduced into the endothermic reactor via the pyrolysis coke, are inert and do not substantially react within the endothermic reactor 22, thus maintaining their particle size.
  • these foreign particles are carried upwards due to the relatively high flow rate of the crude synthesis gas. Due to the conical extension of the endothermic reactor, however, there is a slowing down of the flow velocity of the
  • a height H can be calculated and / or determined, at which the weight of the foreign particles (grains of sand) compensates the upward, mediated by the flow of the synthesis gas force. At this altitude, there is an accumulation or concentration of foreign particles.
  • Side trigger 25 is formed.
  • the side trigger 25 is connected via a line (symbolized as arrow 26) to a jet pump 28.
  • a line symbolized as arrow 26
  • water is used as the pump medium, which is introduced via a line 29 into the jet pump and leaves it via a line 30.
  • Jet pump generated negative pressure are concentrated at the level H particles or foreign particles are withdrawn from the endothermic reactor and removed with the water via the line 30 from the system. It can not be completely avoided that the foreign particles also carry a small proportion of synthesis gas as well as pyrolysis coke particles. However, the proportion thereof is very low compared to the proportion of synthesis gas leaving the endothermic reactor via line 24.
  • discharged substances can be suitably separated from each other, and optionally fed back to the system.
  • the jet pump 28 expediently performs a full quench for the withdrawn mass flow.
  • the amount of laterally drawn mass flow can be variably adjusted.
  • the system according to the invention can continue to be operated by accumulation of inert solid particles, such as sand, without interruption of operation by corresponding actuation of the jet pump 28.
  • inert solid particles such as sand
  • a side trigger prevents melt phase formation, such as Alkali silicates.
  • a jet pump water jet pump
  • a jet compressor gas jet pump
  • a driving medium such as steam or CO 2
  • additives such as kaolin, limestone or dolomite may be added to the endothermic gasifier. The total mixture can then be withdrawn laterally without sticky particles forming.
  • a side take-off can also be provided on comparable run-of-river reactors which serve for endothermic quenching.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Materials Engineering (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Industrial Gases (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

L'invention concerne une installation de gazéification au moins partielle d'une matière de départ organique, comprenant un dispositif de gazéification basse température (1) dans lequel on peut extraire par carbonisation basse température un gaz de carbonisation (B) goudronneux à partir d'une matière de départ (A) organique solide, et un dispositif de gazéification haute température (2) pourvu d'une unité d'oxydation (21) et d'un dispositif de gazéification endothermique (22), le gaz de carbonisation (E) goudronneux pouvant être transformé en gaz de synthèse (D) par oxydation partielle dans l'unité d'oxydation (21) et subséquemment par réduction partielle dans le réacteur endothermique (22) ; le réacteur endothermique (22) ayant une forme évasée en cône dans la direction verticale, cette forme présentant sur au moins une hauteur (H), notamment sur au moins deux hauteurs (H) différentes, au moins un évent latéral destiné à l'évacuation de particules solides indésirables.
EP14781446.1A 2013-10-22 2014-10-07 Procédé et installation de gazéification d'un matériau de départ Withdrawn EP3060632A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE201310017546 DE102013017546A1 (de) 2013-10-22 2013-10-22 Verfahren und Anlage zur Vergasung von Einsatzmaterial
PCT/EP2014/002719 WO2015058837A1 (fr) 2013-10-22 2014-10-07 Procédé et installation de gazéification d'un matériau de départ

Publications (1)

Publication Number Publication Date
EP3060632A1 true EP3060632A1 (fr) 2016-08-31

Family

ID=51663129

Family Applications (1)

Application Number Title Priority Date Filing Date
EP14781446.1A Withdrawn EP3060632A1 (fr) 2013-10-22 2014-10-07 Procédé et installation de gazéification d'un matériau de départ

Country Status (6)

Country Link
US (1) US20160244327A1 (fr)
EP (1) EP3060632A1 (fr)
CN (1) CN105899647A (fr)
AU (1) AU2014339350A1 (fr)
DE (1) DE102013017546A1 (fr)
WO (1) WO2015058837A1 (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2019113626A1 (fr) * 2017-12-12 2019-06-20 Tyre Takers Pty Ltd Installation de pyrolyse

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GB673648A (en) * 1948-01-08 1952-06-11 Directie Staatsmijnen Nl Improvements in or relating to the conversion of finely divided solid carbonaceous material into gas mixtures
US3911836A (en) * 1974-05-23 1975-10-14 Kenard D Brown Incinerator and system for cleaning products of combustion
IT1252838B (it) * 1991-09-18 1995-06-28 Tomadini Gino & C Procedimento potenziato di gassificazione per gassificatori di combustibili solidi e apparecchiatura adottante tale procedimento
DE4139512A1 (de) 1991-11-29 1993-06-03 Noell Dbi Energie Entsorgung Verfahren zur thermischen verwertung von abfallstoffen
DE4209549A1 (de) 1992-03-24 1993-09-30 Vaw Ver Aluminium Werke Ag Verfahren zur thermischen Behandlung von Reststoffen, z.B. zur Trennung und Verwertung von Metallverbunden mit organischen Anteilen, mittels einer Kombination aus Pyrolyse und Vergasung
DE4404673C2 (de) 1994-02-15 1995-11-23 Entec Recycling Und Industriea Verfahren zur Erzeugung von Brenngas
DE102007012452B4 (de) * 2007-03-15 2014-01-16 SynCraft Enegineering GmbH Vergaser
DE102007050929B4 (de) * 2007-10-23 2012-10-25 Lurgi Zimmer Gmbh Verfahren und Vorrichtung zur Erzeugung von Vakuum bei der Herstellung von Polyestern und Copolyestern
CA2781195C (fr) * 2009-11-18 2018-09-18 G4 Insights Inc. Procede et systeme d'hydrogazeification de la biomasse
DE102010018197A1 (de) * 2010-04-26 2011-10-27 Stadtwerke Rosenheim Gmbh & Co. Kg Verfahren und Vorrichtung zur Vergasung von Biomasse
CN202208705U (zh) * 2011-08-25 2012-05-02 上海泽玛克敏达机械设备有限公司 Bgl加压熔渣气化加纯氧非催化部分氧化制取合成气或氢气的装置
CN102899093B (zh) * 2012-11-01 2017-10-17 邰学林 高效清洁煤气化工艺

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See also references of WO2015058837A1 *

Also Published As

Publication number Publication date
AU2014339350A1 (en) 2016-05-12
DE102013017546A1 (de) 2015-04-23
WO2015058837A1 (fr) 2015-04-30
CN105899647A (zh) 2016-08-24
US20160244327A1 (en) 2016-08-25

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