WO2015039731A1 - Procédé et installation servant à gazéifier au moins en partie une matière première organique solide - Google Patents

Procédé et installation servant à gazéifier au moins en partie une matière première organique solide Download PDF

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Publication number
WO2015039731A1
WO2015039731A1 PCT/EP2014/002396 EP2014002396W WO2015039731A1 WO 2015039731 A1 WO2015039731 A1 WO 2015039731A1 EP 2014002396 W EP2014002396 W EP 2014002396W WO 2015039731 A1 WO2015039731 A1 WO 2015039731A1
Authority
WO
WIPO (PCT)
Prior art keywords
synthesis gas
temperature
coke particles
coke
gas
Prior art date
Application number
PCT/EP2014/002396
Other languages
German (de)
English (en)
Inventor
Gerald GAUBE
Ralf Tatschke
Jörg KLEEBERG
Original Assignee
Linde Aktiengesellschaft
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 Aktiengesellschaft filed Critical Linde Aktiengesellschaft
Priority to US14/912,170 priority Critical patent/US20160200991A1/en
Priority to CN201480051807.6A priority patent/CN105658773A/zh
Priority to EP14761792.2A priority patent/EP3046998A1/fr
Priority to AU2014323691A priority patent/AU2014323691A1/en
Publication of WO2015039731A1 publication Critical patent/WO2015039731A1/fr

Links

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
    • C10J3/58—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
    • 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
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • 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
    • C10K1/02—Dust removal
    • C10K1/026—Dust removal by centrifugal forces
    • 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
    • C10J2300/0916—Biomass
    • 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
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • 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
    • 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
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock
    • Y02P20/145—Feedstock the feedstock being materials of biological origin

Definitions

  • the invention relates to a method and a plant for at least partial Verga- solution of solid organic feedstock, in particular of biomass, with a low-temperature gasifier and a high-temperature gasifier.
  • BTL Biomass to Liquids method
  • GTL gas-to-liquids
  • CTL coal-to- Liquids
  • An example of a plant for the production of BTL fuels is in Kiener, C. and Bilas, I .: Synthetic biofuel of the second generation. World's first commercial BTL production plant. Energy 2.0, July 2008, p. 42-44.
  • Processes and plants for the at least partial gasification of solid organic feedstock are also known for example from EP 0 745 114 B1, DE 41 39 512 A1 and DE 42 09 549 A1.
  • the present application relates in this case to such processes or plants which have a low-temperature gasifier and a high-temperature gasifier, as explained below. Compared to other methods, these enable u.a. a lower consumption of feed and have a higher cold gas efficiency.
  • the feedstock such as biomass
  • a gasification agent at temperatures between about 300 ° C and 600 ° C to coke (in the case of biomass so-called biococ) and
  • Smoldering is known to be characterized by substoichiometric oxygen supply and thus incomplete combustion at comparatively low temperatures.
  • the carbonization gas is then transferred to a combustion chamber of the high-temperature gasifier and 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. Heat released by this oxidation causes the temperature to rise to 1,200 ° C. to 2,000 ° C., for example 1,400 ° C. Under such conditions, aromatics, tars and oxo compounds contained in the carbonization gas are completely decomposed. As a result, a synthesis gas is formed, which essentially only contains carbon monoxide, hydrogen, carbon dioxide and water vapor. The synthesis gas can also be referred to as (synthesis) raw gas at this point.
  • 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. Heat released by this oxidation causes the temperature to rise to 1,200 ° C.
  • the synthesis gas produced in this way can be brought into contact with coke from the low-temperature gasifier.
  • the coke may be previously treated separately (e.g., by grinding and sifting) and then introduced into the quench unit.
  • chemical quench By endothermic reactions between coke and synthesis gas (so-called chemical quench) the latter is cooled to a target temperature of about 900 ° C. This also causes a partial conversion of the carbon dioxide to carbon monoxide.
  • the carbon monoxide-rich synthesis gas produced in this way can then be further conditioned.
  • the conditioning includes, for example, a further cooling, dedusting, densification and / or the separation of residual carbon dioxide.
  • the conditioning comprises in particular the separation of residual coke from the synthesis gas. This is accomplished in practice by means of a cyclone and a downstream filter. The residual coke thus separated is then cooled in cooling screws and discharged from the pressure chamber via a container lock. discharged. A portion of the residual coke is introduced via container locks back into the pressure chamber and fed through a dense phase current to the burner (Hochtemperaturvergaser). During the cooling of the synthesis gas, however, there is a condensation of alkalis on the residual coke, so that not all the residual coke can be recycled to avoid too much alkali concentration in Hochtemperaturvergaser. In conventional systems, therefore, a portion of the alkali-loaded residual coke is removed from the system or discarded.
  • the invention is based on a known process for the at least partial gasification of solid organic feedstock, for example biomass.
  • a tarry carbonization gas is obtained by smoldering in a low-temperature gasifier, as explained above.
  • the carbonization gas is then reacted in a high-temperature gasifier by partial oxidation and then partial reduction to a synthesis gas and further processed downstream of the high-temperature gasifier in appropriate treatment facilities.
  • the synthesis gas is cooled after leaving the Hochtemperaturvergasers first in a cooling device to a temperature of about 600-800 ° C.
  • the cooling takes place according to the invention in such a way, ie to a temperature such that a substantial proportion (in particular at least% by weight 10%,% by weight 20%, 30%, 40%, 50%, 60%, 70%, 80% or 90%) of the alkalis present in the synthesis gas remain in the gaseous phase, but coke particles are already no longer sticky.
  • a substantial proportion in particular at least% by weight 10%,% by weight 20%, 30%, 40%, 50%, 60%, 70%, 80% or 90%
  • the alkalis present in the synthesis gas remain in the gaseous phase, but coke particles are already no longer sticky.
  • the stickiness of the coke particles is too pronounced, which can lead to problems in further handling.
  • the actual temperature to which it is cooled may depend on the composition of the feed and / or environmental conditions. To set a suitable temperature can be used on empirical values. It is also conceivable to provide corresponding sensors or measuring devices which detect the phase of the alkalis or the stickiness of the coke particles, and give the detected values to a control device, via which the temperature can be set.
  • the invention is characterized in that a coarse fraction of coke particles is separated from the synthesis gas in a cyclone device provided downstream of the high-temperature gasifier and the cooling device, a fine fraction of the coke particles passing through the cyclone device with the synthesis gas.
  • the fine fraction of coke particles leaves with the synthesis gas containing the gaseous alkalis, the cyclone device and can be removed from the system.
  • the coarse fraction of the coke particles which is substantially alkali-free, can be recycled to the high temperature gasifier.
  • the synthesis gas passing through the cyclone device is further cooled in a cooler provided downstream of the cyclone device.
  • the coke particles of the fine fraction present in the synthesis gas in this case have, for example, diameters of 0.1 to 10 ⁇ m.
  • the alkalis also present in the synthesis gas condense on the surface of these coke particles.
  • a targeted separation of the alkalis takes place on the particles of the fine fraction, which passes through the cyclone device with the synthesis gas stream.
  • the particles of the fine Fraction are particularly well suited for alkali deposition as they have a relatively large surface area with relatively low mass. As a result, a relatively large surface area is available for the condensation, the calorific value loss being relatively low.
  • the coarse fraction of the coke particles in particular taking advantage of gravity, transferred in a buffer tank and then in a vertically arranged standpipe, wherein the height of the standpipe is selected so that in the lower part of a for fluidization tion sufficient pressure is provided to facilitate dense phase conveying and to ensure entry of the coke provided thereby into the high temperature gasifier.
  • the diameter of the standpipe is chosen so that bridging of the coke particles of the coarse fraction can be avoided.
  • the lowest part of the standpipe can be formed with a further reduced diameter, whereby an increase in the flow velocity can be provided, so that the required for the dense phase fluidization fluidization is ensured only in this lowermost region of the standpipe.
  • the residual coke present in the buffer tank or in the standpipe acts as a pressure barrier, so that coke recycled to the lowermost part of the standpipe into the high-temperature gasifier can be conveyed under a suitable delivery pressure.
  • a suitable delivery pressure Compared to the pressure in the cyclone device prevails in the lowest part of the standpipe preferably an overpressure of about 0.2 to 1 bar.
  • recycle of coke over the buffer vessel and standpipe is performed at a temperature substantially equal to the temperature in the cyclone device.
  • coke can be recycled to the high temperature gasifier at a very high temperature, whereby the efficiency of the gasification is improved accordingly, for example, 0.5% to 1%.
  • Figure 1 shows a system which is adapted to carry out a method according to the invention, in a schematic representation.
  • FIG. 1 shows a system which is set up to carry out a method according to the invention and designated overall by 10.
  • the system 10 comprises a low-temperature gasifier 1 and a high-temperature gasifier 2.
  • a feedstock such as biomass such as wood or corresponding waste, as previously explained, be fed (by means of arrow 1 1 illustrated).
  • oxygen can be fed in via a line 12.
  • the low-temperature gasifier 1 is set up to blaze the solid organic feedstock A.
  • the low temperature carburetor 1 externally, for example, with waste heat of Hochtemperaturvergasers 2, to a suitable temperature, for example 300 ° C to 600 ° C, heated.
  • starting torches of the high-temperature gasifier 2 can also be used.
  • a carbonization B can be discharged from the low-temperature carburetor 1 and transferred to the high temperature carburetor 2.
  • the high temperature carburetor 2 is formed in two parts. It comprises an oxidation unit 21 and a quench unit 22.
  • the carbonization gas B is partially oxidized with an oxygen-containing gas supplied, resulting in temperatures of, for example, 1400 ° C. to 2000 ° C.
  • a synthesis gas is obtained.
  • This synthesis gas contained coke particles have due to the high temperature on a strong stickiness.
  • the synthesis gas obtained at the outlet of the high-temperature gasifier 2 is fed to a cooler 30, where it is cooled to a temperature of 600 to 800 ° C., for example.
  • This temperature is chosen so that present in the synthesis gas alkalis remain in a substantial proportion in the gaseous phase, and in the synthesis gas contained coke particles have no more stickiness.
  • the synthesis gas is fed to a cyclone device 4 where a coarse fraction of the residual coke is deposited in a buffer vessel 15, while the synthesis gas, which among other things a fine fraction of Koksparti- no (for example, with diameters 0.1-10 ⁇ ) and receives gaseous alkalis is supplied via a line 17 to a further cooling device 19.
  • the synthesis gas is cooled in such a way, for example, to temperatures of 100 ° C to 200 ° C, so that the alkalis on the particles of the fine fraction of the coke particles condense. This contaminated with alkalies residual coke z. B. by means of (not shown) wet gas scrubbing from the syngas stream.
  • the diameter of the standpipe is chosen so that bridging of the coke particles can be avoided. Preferred diameters of the standpipe here are 300 mm to 1,000 mm.
  • the height h of the standpipe for example 5 to 50 meters, is selected such that a sufficiently large pressure build-up is achieved during fluidization of the coke particles present in the lowest part of the standpipe, so that dense phase conveying by means of a suitable conveying gas (inert gas, For example, C02) can be operated.
  • a suitable conveying gas for example, C02
  • Such a dense phase conveying represents a particularly effective form of conveying the coke back into the high-temperature gasifier.
  • the lowermost part 25a of the standpipe 25 is formed by reducing the diameter so that here the flow rate of the gas supplied for the fluidization is sufficient for the larger above it Cross section but not.
  • the plant shown is thus able to remove specific alkalis from the residual coke.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Industrial Gases (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne un procédé servant à gazéifier au moins en partie une matière première organique solide (A). Ledit procédé consiste à obtenir, par carbonisation, un gaz de carbonisation contenant du goudron à partir de la matière première (A) dans un gazéificateur à basse température (1), puis à transformer le gaz de carbonisation (B) par oxydation partielle dans un gazéificateur à haute température (2) puis par réduction partielle pour obtenir un gaz de synthèse (D), le gaz de synthèse étant ainsi refroidi dans un dispositif de refroidissement (30) prévu en aval du gazéificateur à haute température (2), de sorte que les alcalis présents dans le gaz de synthèse restent dans la phase gazeuse et les particules de coke présentes dans le gaz de synthèse ne montrent déjà plus aucune viscosité et de sorte qu'une fraction grossière des particules de coke est séparée du gaz de synthèse dans un dispositif cyclonique (4) prévu en aval du dispositif de refroidissement (30), une fraction fine des particules de coke passant le dispositif cyclonique (4) avec le gaz de synthèse.
PCT/EP2014/002396 2013-09-18 2014-09-04 Procédé et installation servant à gazéifier au moins en partie une matière première organique solide WO2015039731A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
US14/912,170 US20160200991A1 (en) 2013-09-18 2014-09-04 Process and plant for at least partial gasification of solid organic feed material
CN201480051807.6A CN105658773A (zh) 2013-09-18 2014-09-04 用于至少部分气化固体有机供料的方法和装置
EP14761792.2A EP3046998A1 (fr) 2013-09-18 2014-09-04 Procédé et installation servant à gazéifier au moins en partie une matière première organique solide
AU2014323691A AU2014323691A1 (en) 2013-09-18 2014-09-04 Method and plant for the at least partial gasification of solid organic feedstock

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102013015536.3 2013-09-18
DE102013015536.3A DE102013015536A1 (de) 2013-09-18 2013-09-18 Verfahren und Anlage zur zumindest teilweisen Vergasung von festem, organischen Einsatzmaterial

Publications (1)

Publication Number Publication Date
WO2015039731A1 true WO2015039731A1 (fr) 2015-03-26

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PCT/EP2014/002396 WO2015039731A1 (fr) 2013-09-18 2014-09-04 Procédé et installation servant à gazéifier au moins en partie une matière première organique solide

Country Status (6)

Country Link
US (1) US20160200991A1 (fr)
EP (1) EP3046998A1 (fr)
CN (1) CN105658773A (fr)
AU (1) AU2014323691A1 (fr)
DE (1) DE102013015536A1 (fr)
WO (1) WO2015039731A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3250662A4 (fr) * 2015-01-30 2018-08-08 Lummus Technology Inc. Système hybride à lit fluide de colonne montante pour la collecte, le transport et la régulation de débit de résidus de carbonisation

Families Citing this family (2)

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DE102017210044A1 (de) * 2017-06-14 2018-12-20 Thyssenkrupp Ag Nachbehandlungsanordnung und Verfahren zum Nachbehandeln von zumindest Gasen stromab einer Wirbelschichtvergasung sowie Logikeinheit und Verwendung
DE102019218806A1 (de) * 2019-12-03 2021-06-10 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. Verfahren und Vorrichtung zum Verbrennen von festen Brennstoffen

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WO2000071644A2 (fr) * 1999-05-21 2000-11-30 Ebara Corporation Procede de generation d'electricite par gazeification
EP1136542A1 (fr) * 1998-11-05 2001-09-26 Ebara Corporation Systeme de production d'energie par gazeification d'un materiau combustible
WO2012068931A1 (fr) * 2010-11-24 2012-05-31 National Institute Of Clean-And-Low-Carbon Energy Système de production de produits solides, liquides et gazeux à partir de charbon et d'une biomasse, et procédé associé de production de produits solides, liquides et gazeux

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DE4139512A1 (de) 1991-11-29 1993-06-03 Noell Dbi Energie Entsorgung Verfahren zur thermischen verwertung von abfallstoffen
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CN2180643Y (zh) * 1994-01-27 1994-10-26 中国科学院山西煤炭化学研究所 灰熔聚流化床汽化装置
DE4404673C2 (de) 1994-02-15 1995-11-23 Entec Recycling Und Industriea Verfahren zur Erzeugung von Brenngas
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EP0846748A1 (fr) * 1996-12-03 1998-06-10 Ebara Corporation Methode et appareil pour récupérer de l'energie à partir de déchets
EP1136542A1 (fr) * 1998-11-05 2001-09-26 Ebara Corporation Systeme de production d'energie par gazeification d'un materiau combustible
WO2000071644A2 (fr) * 1999-05-21 2000-11-30 Ebara Corporation Procede de generation d'electricite par gazeification
WO2012068931A1 (fr) * 2010-11-24 2012-05-31 National Institute Of Clean-And-Low-Carbon Energy Système de production de produits solides, liquides et gazeux à partir de charbon et d'une biomasse, et procédé associé de production de produits solides, liquides et gazeux

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3250662A4 (fr) * 2015-01-30 2018-08-08 Lummus Technology Inc. Système hybride à lit fluide de colonne montante pour la collecte, le transport et la régulation de débit de résidus de carbonisation
US10392572B2 (en) 2015-01-30 2019-08-27 Lummus Technology Inc. Standpipe-fluid bed hybrid system for char collection, transport, and flow control

Also Published As

Publication number Publication date
AU2014323691A1 (en) 2016-03-03
EP3046998A1 (fr) 2016-07-27
CN105658773A (zh) 2016-06-08
DE102013015536A1 (de) 2015-03-19
US20160200991A1 (en) 2016-07-14

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