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EP2007854A1 - Procédé et dispositif d'épuration intégrée des gaz chauffés des constituants gazeux et pulvérulents de gaz de synthèse - Google Patents

Procédé et dispositif d'épuration intégrée des gaz chauffés des constituants gazeux et pulvérulents de gaz de synthèse

Info

Publication number
EP2007854A1
EP2007854A1 EP07726772A EP07726772A EP2007854A1 EP 2007854 A1 EP2007854 A1 EP 2007854A1 EP 07726772 A EP07726772 A EP 07726772A EP 07726772 A EP07726772 A EP 07726772A EP 2007854 A1 EP2007854 A1 EP 2007854A1
Authority
EP
European Patent Office
Prior art keywords
reactor
gas
additives
synthesis gas
dust
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Withdrawn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
EP07726772A
Other languages
German (de)
English (en)
Inventor
Oliver Neumann
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.)
Spirit Of Technology AG
Original Assignee
Spot Spirit Of Technology 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 Spot Spirit Of Technology AG filed Critical Spot Spirit Of Technology AG
Publication of EP2007854A1 publication Critical patent/EP2007854A1/fr
Withdrawn legal-status Critical Current

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
    • C10J3/46—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
    • C10J2300/09—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
    • C10J2300/0956—Air or oxygen enriched air
    • 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
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • 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
    • C10J2300/1261—Heating the gasifier by pulse burners
    • 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
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
    • 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

  • thermal gasification processes has essentially produced three different gasifier types, the entrained flow gasifier, the fixed bed gasifier and the fluidized bed gasifier.
  • the entrained flow gasifier For the commercial gasification of biomass, primarily the fixed bed gasifier and the fluidized bed gasifier were further developed.
  • Literature for fluidized-bed gasification which forms part of this application can be found in the following literature: Wolfgang Adlroch, Rheinbraun AG, Hisaaki Sumitomo Heavy Industries, Ltd., Joachim Wolff, Karsten Radtke (Speaker), "High-Temperature Winkler Gasification of Municipal Solid Waste", Krupp Uhde GmbH, Gasification Technology Conference, San Francisco, California, USA; October 8-11, 2000; Conference Proceedings Literature for circulating fluidized bed in the composite system which is part of this application can be taken from the following literature: "Decentralized electricity and heat generation based on biomass gasification", R. Rauch, H. Hofbauer, lecture University of Leipzig 2004.
  • Literature for combination fixed bed (rotary tube) which is part of this application can be taken from the following literature: 30 MV Carbo V Biomass Gasifier for Municipal CHP; The CHP Project for the City of Aachen Dr Rudioff; Lecture Paris October 2005
  • gasification takes place in two stages.
  • the biomass is split at 500 0 C in their volatile and solid components.
  • the result is a tar-containing gas and additionally "charcoal".
  • the gas is burned at temperatures in excess of 1200 ° C, with tars decomposing into CO2 and H2. With the hot flue gas and the Charcoal is then produced a CO and H2-containing product gas.
  • the fluidized bed gasifiers can be subdivided into two processes, which differ in the heating of the fluidized bed, the circulating fluidized bed gasifier and the stationary fluidized bed gasifier.
  • Literature for desulfurization in a fluidized bed gasification which forms part of this application can be found in the following literature: Gasification of Lignite and Wood in the Lurgi Circulating Fluidized Be Gasifier; Research Project 2656-3; Final Report, August 1988, P. Mehrung, H.Vierrath; LURGI GmbH; for Electric Power Research Institute PaIo Alto Californic: ZWS Pressure Gasification in Combination Block Final Report BMFT FB 03 E 6384-A; P. Mehrung LURGI GmbH; Bewag
  • the object of the invention is a method and apparatus for process-integrated hot gas cleaning of dust and gaseous ingredients of a synthesis gas, which in the
  • Gasification occur, especially in the gasification of biomass.
  • the biomass is also gasified in a fluidized bed with steam as the oxidation and fluidizing medium.
  • this is a stationary fluidized bed with two specially developed pulse burners, which allow an indirect heat input into the fluidized bed located in the reactor.
  • the advantage compared to the fixed-bed gasifier and the circulating fluidized bed is the lack of pronounced temperature and reaction zones.
  • the fluidized bed consists of an inert bed material. This ensures a simultaneous sequence of the individual partial reactions and a homogeneous temperature (about 800 ° C.).
  • the process is virtually depressurised (up to a maximum of 0.5 bar) and is therefore technically easy to implement. It is characterized by a high economic efficiency.
  • the acquisition costs are among the aforementioned carburetor types.
  • the starting point for further use as fuel is the medium-calorific gas from the bio-synthesis gas plant (based on renewable raw materials), which after dedusting and scrubbing of condensable hydrocarbons (oil quench) via a turbo compressor to about 20 bar compressed and by the following process steps can be refined:
  • the process of the present invention based on the synthesis gas, is capable of producing 100 tons of biomass 23 tons of high-grade fuel.
  • the inventive method and the corresponding devices require a purification of the generated
  • Pulse burners (including pilot burner) energetically implement.
  • the system is based on the "in situ removal" of the gaseous pollutants in the reaction space of the steam converter or directly in the corresponding one
  • the pollutant components (sulfur) to be removed from the product gas are released directly during the gasification process.
  • An essential component of the presently described process is the direct chemical bonding of these with the components released from the starting materials by the addition of the adsorbent into the gasification reactor. This immediate adsorption immediately after release of the Pollutant components are referred to as "in situ" gas purification (im
  • the goal is the sulfur-containing gas components. (mainly H2S) with the help of aggregates such as limestone, dolomite or similar processed or naturally occurring aggregates.
  • aggregates such as limestone, dolomite or similar processed or naturally occurring aggregates.
  • this method can also be used for the sulfur accompanying substances of the same main group of the periodic table Se (selenium) and Te (Telur).
  • thermodynamic stability of the pollutants prevailing in the vapor splitter directly separates the pollutants sulfur, telur selenium with high efficiency, while the adsorption of chlorine requires more reactive adsorbents and an adaptation to the reaction temperatures.
  • the gaseous pollutant components forming in the reaction of the starting materials are transported to the solid particles of the adsorbents in the form of a two-phase reaction (gas-solid) by convection and diffusion of the pollutant to the adsorbent particle and react thermodynamically there stable salt. These particles are discharged with the grayling or partially separated into the gas purification stages downstream of the gas path, in particular in the multi-cyclone and the sintered metal fine filters, where they are selectively discharged.
  • the goal is the absorption or removal of chlorine, which is present as a chlorine radical and derived from organic chlorine compounds.
  • Other chlorine compounds for example the chlorine salts chlorides
  • chlorine salts chlorides are less relevant in the context of the process according to the invention.
  • the method can be extended to the group of halogens (Cl, J, Br, F) according to the thermodynamic properties of the individual components.
  • the absorbents or reactants are introduced in terms of process technology at the most suitable site for the respective task.
  • the injection into the external cyclone is expedient, especially to find suitable reaction conditions for the case of chlorine absorption.
  • control of the metering of additives takes place either via a ratio control with variable ratio between feedstock and additive or via a trim-back control, the reference variable reflecting the pollutant concentration measured in the synthesis gas.
  • the deposition of dust as a further step in the synthesis gas makes special demands on the deposition of extremely fine, high-carbon dust.
  • This gas purification stage consists of a multicyclone as pre-treatment stage and downstream of a filter unit.
  • the multi-cyclone consists of a battery of small cyclones, which are mounted in a housing on a support plate.
  • the incoming product gas (containing dust and adsorbent), distributed according to the flow resistance almost equally to the individual elements of the multi-cyclone. In these elements, the separation of a partial flow of the dust takes place (together with the adsorbent).
  • the gas leaves the apparatus, the dust collects together with the likewise deposited adsorbent in the funnel of the apparatus, from where the separated substances are discharged.
  • the second stage of this hot gas cleaning and dedusting consists of fine filters with sintered metal candles.
  • dust and laden Adsorbensan At these forms of the candles of the non-separated in the multicyclone stage dust and laden Adsorbensan turnover a filter cake, which causes in addition to the dust separation in particular in the case of the deposition of chlorine-containing pollutants without significant increase in Schadstoffadsorption.
  • Layer thickness and the low flow rate of the cake are essential parameters.
  • Fig. 1 shows the purification steps in a carburetor
  • Pulse burners is operated.
  • Fig. 1 shows a carburetor 11 with impulse burners 12 which are arranged in the central region of the carburetor 11, in order to form in this region a fluidized bed or a fluidized bed, which are preferably formed stationary.
  • the number of pulse burners can be determined variably. There are both one and two or more conceivable.
  • Starting materials 14 are introduced in the region of the pulse burner 12.
  • feedstocks can be biomass and other substances like. Lignite or secondary raw materials (such as municipal waste, Klarschlämme, waste etc from the food industry ..
  • the biomass is gasified in a fluidized bed, consisting of inert bed material in the range of about 800 0 C.
  • the pulse burner Q operated with Q (pkt) (In addition to the synthesis gas (product gas) produced in the reformer, the most varied fuel gas streams (from propane to natural gas and similar gases) can be used as the fuel gas, so that in particular in one Plant combination of these pulse burners for the combustion of so-called off-gases, which can be used as by-products in syntheses such as methanol synthesis, can be used and thus contributes to increasing the efficiency of an entire system.
  • This fuel gas comes in normal operation as a branch of the own production, that is the refining of the biomass to a new product: heating gas ( advicekalorisch).
  • the starting materials 14 additives are added, these may be calcium carbonate, limestone, dolomite or the like. These are inserted immediately in the area 1 of the impulse burner or in the fluidized bed or mixed with the feed before they are introduced into the fluidized bed. Alternatively, they may also be introduced directly into the reactor in the form of calcium carbonate, limestone, calcium hydroxide or the like.
  • the additive is preferably incorporated directly in the upper region of the reactor.
  • an absorption or removal of chlorine which is present as a chlorine radical and is usually derived from organic chlorine compounds by other additives.
  • These other additives are preferably hydrated lime or the like.
  • These additives 3, 4 are preferably injected into the dust separator 17 or the multi-cyclone. Of course, it is also conceivable to inject them directly into the reactor 11 or to add them to the starting materials 14.
  • control or regulation of the addition of the additives is carried out either via a ratio control with variable ratio between feedstock and additive or via a trim-back control, which are measured by sensors reference variables in the synthesis gas, then a conclusion can be made to the pollutants.
  • the dust components are separated.
  • different filters and separators are connected in series. Their residues are returned to the reactor. The return can be done at different locations. Below the pulse burner, above the pulse burner or directly into the Bed of burners.
  • cyclones 17 and multi-cyclones 18 are used, as well as filters, in particular fine filters 19, which may be formed as a downstream battery of sintered metal filters.
  • a cyclone 17 is connected downstream, wherein via a dust separation 21, a return can be done below or above the pulse burner.
  • an intermediate cooling takes place in a cooler 22 to temperatures between 150 and 700 0 C (above the dew point of the synthesis gas), and then cooled to be purified in a multicyclone.
  • the additive hydrated lime or the like can both in the cyclone
  • the synthesis gas is supplied in parallel or in series to a series of fine filters 19.
  • the residues of the fine filter and the multi-cyclone are collected in a dust separator 21 and fed back to the reactor at different points, as already described above.
  • the separated dust above or below the pulse burner can be supplied.

Landscapes

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

Abstract

Procédé d'épuration intégrée d'un gaz de synthèse, comprenant les étapes suivantes : gazéification des matières chargées dans un réacteur via l'utilisation de brûleurs d'impulsion ; ajout d'additifs dans le réacteur ou la rampe de gaz placé en aval du réacteur pour l'élimination de composants gazeux soufrés pour parvenir à une élimination in situ ; séparation des poussières dans le gaz de synthèse dans la rampe de gaz placée en aval ; réintroduction des poussières séparées dans le réacteur.
EP07726772A 2006-04-11 2007-03-09 Procédé et dispositif d'épuration intégrée des gaz chauffés des constituants gazeux et pulvérulents de gaz de synthèse Withdrawn EP2007854A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102006017353A DE102006017353A1 (de) 2006-04-11 2006-04-11 Verfahren und Vorrichtung zur prozessintegrierten heißen Gasreinigung von Staub- und gasförmigen Inhaltsstoffen eines Synthesegases
PCT/EP2007/052257 WO2007118736A1 (fr) 2006-04-11 2007-03-09 Procédé et dispositif d'épuration intégrée des gaz chauffés des constituants gazeux et pulvérulents de gaz de synthèse

Publications (1)

Publication Number Publication Date
EP2007854A1 true EP2007854A1 (fr) 2008-12-31

Family

ID=38190626

Family Applications (1)

Application Number Title Priority Date Filing Date
EP07726772A Withdrawn EP2007854A1 (fr) 2006-04-11 2007-03-09 Procédé et dispositif d'épuration intégrée des gaz chauffés des constituants gazeux et pulvérulents de gaz de synthèse

Country Status (4)

Country Link
US (1) US20090056537A1 (fr)
EP (1) EP2007854A1 (fr)
DE (1) DE102006017353A1 (fr)
WO (1) WO2007118736A1 (fr)

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Also Published As

Publication number Publication date
DE102006017353A1 (de) 2007-10-18
WO2007118736A1 (fr) 2007-10-25
US20090056537A1 (en) 2009-03-05

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