WO2018024404A1 - Installation et procédé de conversion de combustibles contenant du carbone en gaz de synthèse - Google Patents

Installation et procédé de conversion de combustibles contenant du carbone en gaz de synthèse Download PDF

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Publication number
WO2018024404A1
WO2018024404A1 PCT/EP2017/065515 EP2017065515W WO2018024404A1 WO 2018024404 A1 WO2018024404 A1 WO 2018024404A1 EP 2017065515 W EP2017065515 W EP 2017065515W WO 2018024404 A1 WO2018024404 A1 WO 2018024404A1
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WO
WIPO (PCT)
Prior art keywords
gasification
fluidized bed
synthesis gas
reactor
bed zone
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
PCT/EP2017/065515
Other languages
German (de)
English (en)
Inventor
Ralf Abraham
Domenico Pavone
Dobrin Toporov
Peter Marek
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.)
ThyssenKrupp AG
ThyssenKrupp Industrial Solutions AG
Original Assignee
ThyssenKrupp AG
ThyssenKrupp Industrial Solutions 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 ThyssenKrupp AG, ThyssenKrupp Industrial Solutions AG filed Critical ThyssenKrupp AG
Publication of WO2018024404A1 publication Critical patent/WO2018024404A1/fr
Anticipated expiration legal-status Critical
Ceased 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
    • 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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/06—Continuous processes
    • C10J3/18—Continuous processes using electricity
    • 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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • 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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C10J3/56—Apparatus; Plants
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/123—Heating the gasifier by electromagnetic waves, e.g. microwaves
    • C10J2300/1238—Heating the gasifier by electromagnetic waves, e.g. microwaves by plasma

Definitions

  • the present invention relates to a plant for the conversion of carbonaceous fuels into synthesis gas comprising a reactor having at least one fluidized bed zone in which the gasification of the fuels by gasification agent, and at least one downstream in the flow path of the fluidized bed zone, in which by means of at least one plasma torch a gasification of takes place from the fluidized bed emerging fluid stream.
  • HTW method high-temperature Winkler method
  • a fuel also difficult fuels with a very high proportion of ash and biologically based fuels are used.
  • These are introduced into a fluidized bed, which is operated as a bubbling fluidized bed, and gasified with oxygen.
  • the HTW process works in comparison to other gasification processes at comparatively moderate temperatures, at which the resulting ash does not leave the gasification reactor in a molten state. This has operational advantages, especially with corrosive ashes.
  • gasification is usually done via separate nozzles with the gasification agents, such as water vapor, carbon dioxide, oxygen or air.
  • the gasification agents such as water vapor, carbon dioxide, oxygen or air.
  • These nozzles are arranged, for example, in different planes, for example both in the fluidized bed zone and in the so-called freeboard zone (FB).
  • FB freeboard zone
  • FB freeboard zone
  • a high material and energy transfer rate is achieved and the return of the unreacted solids over the cyclone and return line in the fluidized bed, a uniform temperature distribution over the fluidized bed can be secured.
  • the temperature of the fluidized bed should be kept below the temperature of the ash softening point.
  • the proportion of the total oxygen above the fluidized bed is, for example, between about 40% and about 10% in an HTW process.
  • temperatures should preferably not exceed certain limits, and preferably the operating temperature should be at least about 100 ° C below the ash softening point.
  • the addition of oxygen to the post-gasification zone results in partial combustion of the synthesis gas reservoir (CO + H 2 ) and consequent reduction of the synthesis gas yield.
  • EP 0 153 235 B1 likewise describes a process for the production of synthesis gas, in which the gasification first takes place at a moderate temperature of 700 to 800 ° C., working in a fluidized bed.
  • a second so-called conversion reactor is used, in which the exhaust gases are introduced from the gasification reactor.
  • the injected gas is brought to a very high temperature at the entrance of the conversion reactor, to which a plasma torch can be used. The temperature can thereby be brought to 3000 to 5000 ° C in the inlet zone of the second reactor.
  • the second conversion reactor is used in this known method to reduce the proportion of methane and higher hydrocarbons contained in the synthesis gas by reaction with water vapor also contained in the gas stream.
  • the temperature in the conversion reactor is 1200 ° C to 1500 ° C.
  • the disadvantage is that it increases the CGr content in the gas.
  • it is further proposed, on the one hand, to introduce the gas stream from the fluidized bed gasification into the conversion reactor and, on the other hand, to heat another gas via a plasma torch to a very high temperature and to inject it into the conversion reactor.
  • the injected additional gas may be hydrogen or nitrogen. Since two separate reactors are used in this known plant, there is a higher expenditure on equipment.
  • fluidized-bed reactors as well as other types of gasification agent feed are described in the publications DE 10 2007 006 982 B4, AT 503 517 A1, DE 10 2011 051 906 A1, DE 10 2013 107 311 A1 or EP 1 201 731 A1 described.
  • the object of the present invention is to provide a plant and a corresponding process for the conversion of carbonaceous fuels into synthesis gas having the features of the aforementioned type, by means of which different feedstocks in a fluidized bed optionally gas at higher pressures with high safety and availability let and which work economically.
  • the solution of this object provides a plant for the conversion of carbonaceous fuels in synthesis gas with the features of claim 1 and a method having the features of claim 9.
  • At least one plasma torch is arranged such that its flame is discharged into the reactor which has the fluidized bed zone.
  • the plant thus comprises a reactor in which both the fluidized bed gasification takes place as well as the gasification by means of at least one plasma torch.
  • the fluidized-bed gasification may also take place by means of at least one plasma burner.
  • the use of a plasma burner gives a better conversion of the volatile substances, but saves the gasification agent oxygen. Since both processes run in only one reactor, this is achieved with a reduced expenditure on equipment.
  • the costs of producing pure oxygen in a conventional HTW gasification process are extremely high and therefore significantly affect the economics of the HTW gasification process.
  • Pure oxygen is obtained, for example, by cryogenic air separation.
  • the supplied air must be filtered, compressed and cooled to approx. - 185 ° C.
  • the liquefied air stream must then be distilled in distillation towers. Thereafter, the separation takes place depending on the boiling point in individual components. Therefore, the solution according to the invention is advantageous because the otherwise used oxygen lances can be completely or partially replaced by plasma torches in the inventive method.
  • the region in which the gasification takes place is arranged in the same reactor above the fluidized bed zone. This makes it possible to work with two different temperature zones in one reactor, wherein the temperature in the fluidized bed zone is lower than in the region of the post-gasification.
  • the at least one plasma torch for example, at least partially disposed in the wall of the reactor, which also has the at least one fluidized bed zone.
  • the plasma burner (s) may be arranged such that the plasma / flame is discharged into the reactor in an approximately radial direction with respect to the reactor and / or approximately transversely to the flow direction of the fluid in the region of the post-gasification.
  • the plasma torch (s) is / are preferably arranged such that the plasma / flame is released into the reactor above the fluidized bed zone.
  • the fluid flow exiting from the fluidized bed zone upwards is then preferably acted upon by the flame of the plasma burner approximately transversely to its direction of flow.
  • the region of the reactor in which the gasification takes place is approximately cylindrical and / or the reactor is in the region of the fluidized bed zone approximately conically widening in the flow direction of the fluid.
  • a preferred embodiment of the invention provides that the system comprises a downstream in the flow path the region in which the gasification takes place cyclone separator. After passing through the region of the post-gasification, a separation of solids can then take place in this cyclone separator, and subsequently the thus purified fluid stream can be returned to the fluidized bed zone via a return line leaving the cyclone separator, which discharges into the fluidized bed zone of the reactor, so that both the Be traversed area of the fluidized bed and the gasification zone.
  • the present invention further relates to a process for the conversion of carbonaceous fuels in synthesis gas, wherein in a reactor having at least one fluidized bed zone, a gasification of the fuels by gasification, wherein in at least one downstream in the flow path of the fluidized bed zone by means of at least one plasma burner, a gasification of
  • the gasification by means of the at least one plasma burner takes place in the reactor, which comprises the fluidized-bed zone.
  • the gasification in the region which is acted upon by at least one plasma torch at a higher temperature than the gasification in the fluidized bed zone.
  • the gasification takes place in the fluidized bed zone at a temperature of about 750 ° C to 850 ° C and the gasification at a temperature higher by at least about 100 ° C, preferably at a temperature of at least about 900 ° C, more preferably at a temperature in Range from about 950 ° C to about 1200 ° C.
  • two different temperature zones are formed, namely the fluidized-bed zone with temperatures of, for example, around 800 ° +/- about 50 ° C. and the post-gasification zone with, for example, about 1000 ° C. +/- about 100 ° C.
  • the flame of the plasma torch for example, a maximum temperature in the flame kernel of about 3500 ° C to about 4500 ° C.
  • the at least one plasma torch can be operated with at least one reducing and / or at least one oxidizing gas.
  • the at least one plasma torch may be operated with a fluid stream comprising at least one of the fluids selected from steam, air, oxygen, nitrogen and CO2.
  • the use of steam is advantageous because its production is particularly cost-effective, and it is particularly reactive.
  • the flame of the plasma torch contains radicals such as 0, H, OH, O 2 , H 2 and H 2 O and a temperature of, for example, in the range of about 4000 ° C.
  • the very hot local flame temperature and the high supply of highly reactive radicals tars and hydrocarbons can be cracked.
  • the increased synthesis gas temperature and the conversion of the bed material are positively influenced by the heterogeneous reaction of steam and C0 2 .
  • the plasma temperature can preferably be controlled by injecting steam and / or C0 2 in the region of the plasma burner.
  • the gasification is preferably carried out in a pressure-charged fluidized bed, wherein the gasification in the fluidized bed zone preferably at a pressure of at least about 1 bar, in particular of at least about 5 bar to about 40 bar.
  • Figure 1 is a schematically simplified view of a system according to the invention in partial longitudinal section;
  • Figure 2 is an enlarged detail of a detail II of Figure 1;
  • FIG. 3 shows a schematically simplified illustration of a plasma burner which can be used in the context of the present invention.
  • the plant comprises a reactor 10, in which the gasification of the carbonaceous fuels takes place.
  • This reactor 10 comprises a fluidized bed zone I I in a lower conically widening section.
  • the fuel is supplied to the fluidized bed, for example via a supply device 17 arranged laterally there, which is indicated here only schematically by an arrow.
  • various feed devices such as lines and / or nozzles are further provided on the reactor 10, by means of which the supply of the gasification agent takes place, these feeders are only schematically indicated by arrows.
  • These are for example a plurality of feed devices 18 a, 18 b for oxygen and / or steam, which may be arranged at different height intervals to the lower end of the fluidized bed zone 11 and spaced from each other on the reactor 10.
  • a feed device 19 for CO2 for example, in the lower end of the fluidized bed zone 11 is provided, with multiple accesses for CO2 may be present.
  • one or two ash deductions for the supply of CO2 can be provided in the fluidized bed.
  • a plasma torch 13 is arranged, which emits its flame approximately in the radial direction in the interior of the reactor 10 into it, so that the flame of the plasma torch 13 approximately in the transverse direction relative to the axial flow of the Fluid which flows in the reactor in the region of the gasification in the longitudinal direction of the reactor 10 upwards.
  • a connecting line 21 At the upper end of the fluid flow exits the reactor from the side and passes through a connecting line 21 into a cyclone separator 15, in which a separation of solid fractions can be done.
  • the separated solids emerge downwards from the cyclone separator 15 and flow back via the return line 16, this return line 16 discharging downstream in the area of the fluidized bed zone 11 into the reactor 10, so that the separated solids are reintroduced into the fluidized bed zone and there again a Gasification can be supplied.
  • the purified gas stream can be removed from the circulation.
  • FIG. 2 shows an enlarged detail view of the section of FIG. 1 designated by II.
  • the plasma torch 13 in the wall 14 of the reactor can be seen on an enlarged scale, the plasma torch 13 being illustrated only schematically here. It can be seen that the flame / plasma 23 enters the interior of the reactor from the lateral wall 14 in approximately a radial direction, preferably at a certain distance above the upper end of the fluidized bed zone 11 of the reactor 10.
  • a plasma burner 13 which can be used by way of example in a system according to the present invention will be explained in more detail below with reference to FIG.
  • This comprises an approximately cylindrical housing 24, for example, in which a ring-shaped electrode 26 is supplied via a power supply device 25.
  • This electrode concentrically surrounds a magnet 30, which generates a magnetic field.
  • approximately annular cooling device 27 is provided for the cooling of the magnet 30.
  • a plasma column 31 is generated.
  • the inside of the housing 24 is supplied from the outside radially a process gas 28, which then flows with the plasma column 31 in the axial direction in the housing and enters a nozzle 29, from which then the hot process gas, as indicated by the arrows 23 in Figure 3, emerges.
  • Such a hot process gas then passes as a flame 23 of the plasma torch 13, as described above with reference to Figure 2, in the reactor 10th

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

Abstract

La présente invention concerne une installation de conversion de combustibles contenant du carbone en gaz de synthèse, comprenant un réacteur (10), doté d'au moins une zone de lit fluidisé (11), dans laquelle une gazéification de combustibles, au moyen d'un agent de gazéification, se déroule, et d'au moins une zone (12) en aval dans la voie d'écoulement de la zone de lit fluidisé (11), dans laquelle, au moyen d'au moins un chalumeau à plasma (13), une post-gazéification de flux de fluide sortant de la zone de lit fluidisé (11) se déroule. Selon l'invention, l'au moins un chalumeau à plasma (13) est disposé de sorte que sa flamme est distribuée dans le réacteur (10), lequel comporte la zone de lit fluidisé (11). L'invention concerne une installation de conversion de combustibles contenant du carbone en gaz de synthèse, au moyen de laquelle les différentes matières premières peuvent être gazéifiées dans un lit fluidisé, le cas échéant, à des pressions plus élevées, avec une grande sécurité et disponibilité. L'utilisation d'un chalumeau à plasma (13) permet une meilleure conversion de substances volatiles et permet des économies de l'oxygène autrement utilisé en tant qu'agent de gazéification coûteux lors de la post-gazéification.
PCT/EP2017/065515 2016-08-02 2017-06-23 Installation et procédé de conversion de combustibles contenant du carbone en gaz de synthèse Ceased WO2018024404A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102016214242.9A DE102016214242B4 (de) 2016-08-02 2016-08-02 Anlage und Verfahren zur Umwandlung kohlenstoffhaltiger Brennstoffe in Synthesegas
DE102016214242.9 2016-08-02

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WO2018024404A1 true WO2018024404A1 (fr) 2018-02-08

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111057585A (zh) * 2018-10-17 2020-04-24 中国石油化工股份有限公司 煤流化气化的方法

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2756160C1 (ru) * 2020-12-11 2021-09-28 Федеральное государственное бюджетное учреждение высшего образования «Тамбовский государственный технический университет» (ФГБОУ ВО «ТГТУ») Способ получения синтез-газа из биоотходов
DE202022000489U1 (de) 2022-02-25 2022-05-16 Ralf Abraham Vorrichtung zur Produktion von Synthesegas aus biogenen Rest- und Abfallstoffen

Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4469508A (en) * 1982-04-30 1984-09-04 Electricite De France (Service National) Process and installation for heating a fluidized bed by plasma injection
DE3537758A1 (de) 1985-10-21 1987-04-23 Korf Engineering Gmbh Verfahren zur erzeugung von co- und h(pfeil abwaerts)2(pfeil abwaerts)-haltigem gas und vorrichtung zu dessen durchfuehrung
EP0153235B1 (fr) 1984-02-16 1989-01-18 Framatome Procédé de production de gaz de synthèse
US5958264A (en) 1996-10-21 1999-09-28 Pyrogenesis Inc. Plasma gasification and vitrification of ashes
EP1201731A1 (fr) 2000-10-26 2002-05-02 RWE Rheinbraun Aktiengesellschaft Procédé de gazéification en lit fluidisé de solides contenant du carbone et installation de gazéification
AT503517A1 (de) 2002-11-04 2007-10-15 New Plasma Gmbh & Co Keg Verfahren zum aktivieren, insbesondere vergasen, von kohlenstoff enthaltenden substanzen
DE102007006982B4 (de) 2007-02-07 2009-03-19 Technische Universität Bergakademie Freiberg Verfahren und Vorrichtung zur Vergasung fester Brennstoffe in der Wirbelschicht unter erhöhtem Druck
US20120091395A1 (en) * 2008-07-08 2012-04-19 Karl-Heinz Tetzlaff Method and Device for Producing Low-Tar Synthesis Gas from Biomass
DE102011051906A1 (de) 2011-07-18 2013-01-24 Technische Universität Bergakademie Freiberg Verfahren und Vorrichtung zur Vergasung kohlenstoffhaltiger fester Stoffe mit Wasserdampf und Kohlendioxid und deren Gemische
DE102013107311A1 (de) 2013-07-10 2015-01-15 Thyssenkrupp Industrial Solutions Ag Verfahren und Vorrichtung zur Nachbehandlung des bei der Vergasung anfallenden C-haltigen Bodenproduktes
CN105219443A (zh) * 2015-10-28 2016-01-06 武汉天和技术股份有限公司 等离子流化床气化炉及其处理生物质的工艺

Patent Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4469508A (en) * 1982-04-30 1984-09-04 Electricite De France (Service National) Process and installation for heating a fluidized bed by plasma injection
EP0153235B1 (fr) 1984-02-16 1989-01-18 Framatome Procédé de production de gaz de synthèse
DE3537758A1 (de) 1985-10-21 1987-04-23 Korf Engineering Gmbh Verfahren zur erzeugung von co- und h(pfeil abwaerts)2(pfeil abwaerts)-haltigem gas und vorrichtung zu dessen durchfuehrung
US5958264A (en) 1996-10-21 1999-09-28 Pyrogenesis Inc. Plasma gasification and vitrification of ashes
EP1201731A1 (fr) 2000-10-26 2002-05-02 RWE Rheinbraun Aktiengesellschaft Procédé de gazéification en lit fluidisé de solides contenant du carbone et installation de gazéification
AT503517A1 (de) 2002-11-04 2007-10-15 New Plasma Gmbh & Co Keg Verfahren zum aktivieren, insbesondere vergasen, von kohlenstoff enthaltenden substanzen
DE102007006982B4 (de) 2007-02-07 2009-03-19 Technische Universität Bergakademie Freiberg Verfahren und Vorrichtung zur Vergasung fester Brennstoffe in der Wirbelschicht unter erhöhtem Druck
US20120091395A1 (en) * 2008-07-08 2012-04-19 Karl-Heinz Tetzlaff Method and Device for Producing Low-Tar Synthesis Gas from Biomass
DE102011051906A1 (de) 2011-07-18 2013-01-24 Technische Universität Bergakademie Freiberg Verfahren und Vorrichtung zur Vergasung kohlenstoffhaltiger fester Stoffe mit Wasserdampf und Kohlendioxid und deren Gemische
DE102013107311A1 (de) 2013-07-10 2015-01-15 Thyssenkrupp Industrial Solutions Ag Verfahren und Vorrichtung zur Nachbehandlung des bei der Vergasung anfallenden C-haltigen Bodenproduktes
CN105219443A (zh) * 2015-10-28 2016-01-06 武汉天和技术股份有限公司 等离子流化床气化炉及其处理生物质的工艺

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111057585A (zh) * 2018-10-17 2020-04-24 中国石油化工股份有限公司 煤流化气化的方法

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DE102016214242A1 (de) 2018-02-08

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