EP0310584A2 - Epuration de gaz brut - Google Patents

Epuration de gaz brut Download PDF

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Publication number
EP0310584A2
EP0310584A2 EP88850323A EP88850323A EP0310584A2 EP 0310584 A2 EP0310584 A2 EP 0310584A2 EP 88850323 A EP88850323 A EP 88850323A EP 88850323 A EP88850323 A EP 88850323A EP 0310584 A2 EP0310584 A2 EP 0310584A2
Authority
EP
European Patent Office
Prior art keywords
gas
process according
secondary stage
stage
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.)
Granted
Application number
EP88850323A
Other languages
German (de)
English (en)
Other versions
EP0310584A3 (en
EP0310584B1 (fr
Inventor
Clas Ekström
Bengt-Göran Espenäs
Waclaw Kowalic
Erik Rensfelt
Lars Waldheim
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.)
TPS Termiska Processer AB
Original Assignee
Studsvik AB
TPS Termiska Processer AB
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 Studsvik AB, TPS Termiska Processer AB filed Critical Studsvik AB
Priority to AT88850323T priority Critical patent/ATE88210T1/de
Publication of EP0310584A2 publication Critical patent/EP0310584A2/fr
Publication of EP0310584A3 publication Critical patent/EP0310584A3/en
Application granted granted Critical
Publication of EP0310584B1 publication Critical patent/EP0310584B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime 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
    • C10J3/72—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
    • C10K1/20—Purifying combustible gases containing carbon monoxide by treating with solids; Regenerating spent purifying masses
    • 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
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
    • C10K3/023—Reducing the tar content
    • 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
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • C10J2300/0986—Catalysts

Definitions

  • This invention relates to a process for the refining of a raw gas produced from a carbonaceous material by means of a gasification process in which the refing takes place in a secondary stage separated from the gasifier of the gasifi­cation process.
  • a raw gas produced from different kinds of biofuels and used as a fuel gas is a valuable oil substitute for demanding applications in which the process demands make direct solid fuel fireing impossible, e.g. fireing of lime kilns or conversion of existing oil fired boilers.
  • tar is always present in a raw gas produced by gasification of a carbonaceous mate­rial, e.g. coal, peat, bark, wood or RDF, which limits the utilization to combustion of hot gas in direct or close con­nection to the gasifier.
  • Operational disturbances caused by tarcoating on apparatuses and armatures are a great problem which limits the availability.
  • nitrogen and in certain cases also sulphur (e.g.
  • the object of the presented invention is to provide a raw gas refining process, by means of which the above men­tioned problems will be solved to a great extent.
  • the invention thus concerns a process for the refining of a tar and ammonia containing raw gas, in special cases also containing considerable quantities of hydrogen chloride, the gas being produced by means of an arbitrary gasification process from a carbonaceous material, e.g. bark, wood, peat or Refuse Derived Fuel, RDF, wherein in a secondary stage conversion takes place in contact with an appropriate active (catalytic and possible absorbing) material, e.g. dolomite, of the tar and ammonia present in the raw gas, preferably to such a level that the remaining contents are below 500 and 300 mg/Nm3 respectively.
  • an appropriate active (catalytic and possible absorbing) material e.g. dolomite
  • the secondary stage consists of a Cir­culating Fast Fluidized Bed (CFB) with a bed material at least mainly in form of an active material, e.g. dolomite.
  • CFB Cir­culating Fast Fluidized Bed
  • the secondary stage also could be in­tegrated with an arbitrary CFB-gasifier, only preceded by a primary particle separator, or another type of gasifier.
  • carbonaceous material also contains sulphur in considerable amounts, which e.g. is the case for peat, absorption of hydrogen sulphide on the catalytic and absorb­ing material will of course also take place.
  • the amount of active material which is required in relation to the raw gas amount is determined by the required space-velocity for catalytic conversion of tars and ammonia and depends on several parameters such as the temperature, the residence time of the gas, the particle size of the ac­tive material, the partial pressure of reactants and the de­gree of deactivation of the active material. Too low tempera­ture and/or CO2 partial pressure can result in the tar con­version causing carbon deposition on the active surface, which results in deactivation. If this occurs the material can be activated by treatment with an oxidizing gas, e.g. air and/or steam. Absorption of HCl (and/or H2S) takes place so rapidly at the temperatures of interest that these reactions become almost determined by the equilibrium and result in a consumption of active material corresponding to the formed solid chloride (and sulphide resp.).
  • an oxidizing gas e.g. air and/or steam. Absorption of HCl (and/or H2S) takes place so rapidly at the temperatures of
  • Such a bed is able to handle dust entrained from the gasifier, gives very uniform temperatures in the reaction zone and also gives a homogeneous contact between gas and bed material, that is to say little risk for variations in con­version/absorption degree. Further, the particle size can be varied downwards to a great extent, for those cases in which this is needed to give increased conversion at a given tempe­rature and space-velocity. Considerable erosion of the bed material also results in increased accessible active surface. Also, a secondary stage designed as a CFB with advantage can be integrated with an arbitrary CFB gasifier, which merely has a primary particle separator, or another type of gasi­fier. One also achieves relatively small diameters when scaling up, since the gas velocities can be kept relatively high, up to about 10 m/s, preferably up to 6 m/s.
  • the gasifier consists of a CFB gasifier
  • a connection directly after primary dust separation can thus be made.
  • the secondary stage can in an advantageous manner be integrated with the gasifier, e.g. so that dust from a secondary particle separator after the secondary stage is totally or partly recycled to the gasifier. In this way, the total losses of bed material also become lower, and one also obtains the advantage of using only one type of bed material.
  • the necessary amount of active material in the reactor shaft of the secondary stage for sufficient catalytic conver­sion of tar and ammonia is controlled by the totally added amount and by controlled recirculation of bed material. Re­quired conversion determines suitable combination of tempera­ture, particle size and amount of active material. Because of abrasion, deactivation and/or absorption of HCl (and possibly H2S) consumed active material is replaced by adding corre­sponding amounts of fresh active material and/or activated such material. The residence time of the gas can be controll­ed by the combination diameter/height above the gas inlet.
  • the active material entrained by the outlet gas from the secondary stage means that the HCl absorption is improved, since thermodynamically it becomes more far-reaching at lower temperatures, under the condition that the refined gas is cooled down to an essentially lower temperature before final dust removal.
  • a gasifier 3 which consists of a cir­culating fast fluidized bed (CFB).
  • CFB fast fluidized bed
  • This comprises a reactor 51, a primary separator 52 and recirculation means 53 for bed material separated in the primary separator.
  • the bed material consists of an active catalytic and absorbing material, pre­ferably in the form of dolomite, mixed with ungasified car­bonaceous material, char.
  • the primary separator 52 is a mechanical separator of non-centrifugal type, suitably a U-beam separator, in accordance with what is described in our European Patent EP 0 103 613, relating to a CFB boiler and hereby referred to.
  • the hot raw gas 2 produced in the gasifier 3 is with­drawn directly from the primary separator 52 and is fed di­rectly to a gas cleaning secondary stage 25 without any addi­tional dust removal.
  • the secondary stage 25 is designed as a circulating fast fluidized bed (CFB) 26 and has the same kind of active bed material as the gasifier 3.
  • the raw gas 2 is supplied to the secondary stage 25 so that it constitutes a fluidizing gas.
  • the secondary stage 25 is designed with a long and narrow reactor shaft with arbitrary cross section (e.g. cir­cular or square). Bed material which follows with the gas stream out form the top of the reactor shaft is separated to a major part in a primary particle separator 27, preferably a U-beam separator of the same kind as the U-beam separator of the gasifier, followed by a secondary separator 28, preferab­ly a cyclone.
  • the material 30 separated in the primary par­ticle separator is recycled to the lower part of the circu­lating bed 26 through a recirculation facility.
  • the material 29 separated in the secondary particle separator 28 is added mainly to the lower part of the gasifier 3, stream 31. When needed, a part of the material stream 29 also can be supplied to the lower part of the circulating bed 26, stream 34, and/or be discharged out of the system, stream 43.
  • a side feeding device 15 located on a suitable height is used.
  • Consumed and/or deactivated bed material 35 is discharged by means of a discharging device 36 located in connection with the bottom of the secondary stage 25.
  • the active material used in the secondary stage in this example consists of a calcium-magnesium carbonate con­taining material, preferably dolomite, with a particle size smaller than 2 mm, preferably smaller than 1 mm, which in combination with the passing gas forms the fast circulating fluidized bed 26.
  • the gas velocity in the upper section of the reactor shaft, calculated on the free cross section, is adjusted so that it is below 10 m/s, preferably not above 6 m/s.
  • the fluidizing gas of the fast circulating bed 26 con­sists of the raw gas 2 and added oxidizing gas 13, e.g. air.
  • additional oxidizing gas 33 can be added to the secondary stage 25 on one or on several other suitable, higher located levels.
  • Conversion of tar and ammonia contained in the raw gas 2 and absorption of chloride contained in the raw gas take place by means of contact with the catalytic and absorbing material in the circulating bed 26 within a temperature in­terval of 600-1000°C, preferably 700-900°C or most preferably 850-950°C.
  • the required temperature level is maintained by burning combustible gas components inside the secondary stage 25, which is controlled by adjustment of the amount of added oxidizing gas, streams 13 and 33.
  • the average suspension density in the reactor shaft of the secondary stage 25 is maintained within an interval of 20-300 kg/m3, preferably within an interval of 80-250 kg/m3, so that a necessary contact between the passing gas and the active material is obtained. This is achieved by adjusting the total amount of circulating material in combination with controlling the flow rate of recycled material 30 and 34.
  • the residence time of the gas in the reactor shaft, calculated on an empty reactor shaft, is maintained within an interval of 0.2-20 s, preferably within an interval of 0.5-7 s.
  • activation of deactivated catalytic and absorbing material can be performed by adding oxidizing gas 32, e.g. air, to the material which is recycled to the lower part of the circulating bed, streams 30 and 34.
  • oxidizing gas 32 e.g. air
  • the amount of added oxidizing gas 32 is controlled so that the activation takes place within a temperature interval of 600-1000°C, pre­ferably within an interval of 750-900°C.
  • the refined gas stream 4 leaving the secondary separa­tor 28 of the secondary stage 25 is relieved from entrained finely divided bed material and steam in the subsequent gas treatment stages.
  • the gas passes through two heat exchangers.
  • heat exchange takes place with oxi­dizing gas, stream 10, intended for both the gasifier 3 and the secondary stage 25, so that preheated oxidizing gas 11 at the outlet from the heat exchanger 37 has a suitable tempera­ture, preferably about 400°C.
  • the preheated oxidizing gas 11 is used both in the gasifier 3 (among others as fluidizing gas), stream 12, and in the secondary stage 25, streams 13, 32 and 33.
  • the tempe­rature of the gas 5 is lowered to a level which permits the outlet gas 6 to be further cleaned by using e.g. standard textile filters or a cyclone for further dust removal, at 39, i.e. preferably down to 150-300°C.
  • the removed dust 18 is withdrawn from the dust removal stage 39.
  • the gas stream 4 contains en­trained finely divided active material which follows with the gas stream out of the secondary separator 28.
  • the raw gas 2 from the gasifier contains considerable amounts of HCl. Since absorption of HCl on calcareous materials, such as do­lomite, is favoured by sinking temperature, the gas cooling in the heat exchangers 37 and 38 contributes to increase the degree of absorption of residual HCl on the entrained mate­rial.
  • a scrubber 40 in which it is re­lieved from moisture and other water soluble components.
  • both moistening of the gas stream 7 and con­densation of steam take place.
  • water soluble gas components e.g. NH3, HCl and/or NH4Cl
  • the water stream 20 leaving the scrubber 40 is recir­culated by a pump 41, whereby it is cooled in a heat ex­changer 42, so that the temperature of the water 19 recycled to the scrubber 40 is kept within the interval 15-20°C. Ex­cess water 21 is drained from the water circuit.
  • the gas 8 leaving the scrubber can for industrial app­lications be regarded as pure, i.e. it is almost free from tars, ammonia, dust, HCl and H2S. However, at the present outlet temperatures (about 30°C) it is saturated with steam. Depending on the application, in order to decrease the rela­tive humidity, the gas stream 8 can be preheated or passed through an additional drying stage in order to reduce its moisture content.
  • the pure gas satisfies the requirements for engine operation, e.g. by means of turbocharged diesel engines, and can be burned without any subsequent exhaust gas cleaning.
  • the scrubber 40 can be omitted, so that the refined gas can be utilized either directly after the heat exchanger 37, stream 22, or after the dust separator 39, stream 23.
  • the total pressure drop of the oxidizing gas supplied, e.g. air, at the passage through the production loop, is slightly above 1 bar. This sets requirements on using a com­pressor 16, which increases the oxidizing gas pressure in stream 9 to the pressure level in stream 10 necessary in view of the purpose involved.

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  • 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)
  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)
  • Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
  • Control And Other Processes For Unpacking Of Materials (AREA)
  • Fats And Perfumes (AREA)
  • Artificial Filaments (AREA)
  • Transition And Organic Metals Composition Catalysts For Addition Polymerization (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)
  • Carbon And Carbon Compounds (AREA)
EP88850323A 1987-10-02 1988-09-28 Epuration de gaz brut Expired - Lifetime EP0310584B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT88850323T ATE88210T1 (de) 1987-10-02 1988-09-28 Reinigung von rohgas.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
SE8703816 1987-10-02
SE8703816A SE459584B (sv) 1987-10-02 1987-10-02 Foerfarande foer foeraedling av raagas framstaelld ur ett kolhaltigt material

Publications (3)

Publication Number Publication Date
EP0310584A2 true EP0310584A2 (fr) 1989-04-05
EP0310584A3 EP0310584A3 (en) 1990-03-14
EP0310584B1 EP0310584B1 (fr) 1993-04-14

Family

ID=20369746

Family Applications (1)

Application Number Title Priority Date Filing Date
EP88850323A Expired - Lifetime EP0310584B1 (fr) 1987-10-02 1988-09-28 Epuration de gaz brut

Country Status (15)

Country Link
EP (1) EP0310584B1 (fr)
JP (1) JP2573681B2 (fr)
AT (1) ATE88210T1 (fr)
AU (1) AU612199B2 (fr)
CA (1) CA1335694C (fr)
DE (1) DE3880253T2 (fr)
DK (1) DK175009B1 (fr)
ES (1) ES2039698T3 (fr)
FI (1) FI95924C (fr)
GE (1) GEP19980893B (fr)
LT (1) LT3842B (fr)
LV (1) LV11188B (fr)
NO (1) NO302422B1 (fr)
SE (1) SE459584B (fr)
WO (1) WO1989002909A1 (fr)

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0421468A1 (fr) * 1989-10-05 1991-04-10 Nkk Corporation Oxydation catalytique de l'ammoniac
US5139756A (en) * 1989-10-05 1992-08-18 Nkk Corporation Catalytic oxidation of ammonia
WO1993020245A1 (fr) * 1992-03-27 1993-10-14 Still Otto Gmbh Procede combine de production de coke metallurgique et d'eponge de fer
EP0629684A1 (fr) * 1993-06-17 1994-12-21 Texaco Development Corporation Procédé d'oxydation partielle pour produire un courant de gaz purifié chaud
EP0629685A1 (fr) * 1993-06-17 1994-12-21 Texaco Development Corporation Procédé d'oxydation partielle pour produire un courant de gaz purifié chaud
EP0628621A3 (fr) * 1993-06-11 1995-02-15 Enviropower Oy Méthode et réacteur pour le traitement d'un gaz industriel.
NL1001555C2 (nl) * 1995-10-27 1997-05-02 Biomass Technology Group B V Werkwijze voor de katalytische behandeling van een gasmengsel.
DE19907901C2 (de) * 1999-02-24 2001-11-29 Mg Technologies Ag Verfahren zur katalytischen Spaltung von flüchtigen höheren Kohlenwasserstoffen
WO2010034791A1 (fr) * 2008-09-26 2010-04-01 Siemens Vai Metals Technologies Gmbh & Co Procédé et dispositif de dépoussiérage et d'épuration à sec d'un gaz produit lors de la fabrication de fonte ou de gazéification de charbon
WO2010037465A1 (fr) * 2008-09-30 2010-04-08 Uhde Gmbh Epuration de gaz chaud
WO2014183847A1 (fr) * 2013-05-16 2014-11-20 Ecoloop Gmbh Procédé de purification de gaz de synthèse

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5543390A (en) 1990-11-01 1996-08-06 State Of Oregon, Acting By And Through The Oregon State Board Of Higher Education, Acting For And On Behalf Of The Oregon Health Sciences University Covalent microparticle-drug conjugates for biological targeting
US5827819A (en) 1990-11-01 1998-10-27 Oregon Health Sciences University Covalent polar lipid conjugates with neurologically active compounds for targeting
DE102010024429A1 (de) * 2010-06-21 2011-12-22 Technische Universität München CO2 freies IGCC Kraftwerk mit Heißgasreinigung und optimierter CO2 Abtrennung
CN103154210B (zh) 2010-08-16 2015-07-22 能源与环境研究中心基金会 零残留碳排放的高效转化碳质燃料为清洁合成气的夹心气化方法
CN103820170B (zh) * 2014-02-21 2015-09-02 陕西延长石油（集团）有限责任公司碳氢高效利用技术研究中心 一种粗煤气中焦油组份及含碳颗粒的转化装置及方法
JP6345139B2 (ja) * 2015-03-13 2018-06-20 三菱日立パワーシステムズ株式会社 ガスエンジンシステム

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3807090A (en) * 1970-12-02 1974-04-30 Exxon Research Engineering Co Purifications of fuels
US4273749A (en) * 1977-06-03 1981-06-16 Hitachi, Ltd. Refining process of hot gas containing hydrogen sulfide and ammonia
DE3017998C2 (de) * 1980-05-10 1994-05-26 Krupp Koppers Gmbh Verfahren zur katalytischen Behandlung von Partialoxidationsrohgas
DE3404483A1 (de) * 1984-02-08 1985-08-08 Environment Protecting Engineers, Inc., Southfield, Mich. Verfahren zum reinigen von pyrolysegasen und vorrichtung zur durchfuehrung dieses verfahrens
SE457355B (sv) * 1985-09-25 1988-12-19 Skf Steel Eng Ab Saett att framstaella en ren, koloxid och vaetgas innehaallande gas
SE8600639L (sv) * 1986-02-13 1987-08-14 Goetaverken Energy Syst Ab Forfarande och anordning for stoftrening vid generering av gas for drift av mesaugnar
DE3716199A1 (de) 1987-05-14 1988-11-24 Linde Ag Verfahren und vorrichtung zur reinigung von rohgasen unter gleichzeitiger gewinnung von synthese- und brenngas

Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5139756A (en) * 1989-10-05 1992-08-18 Nkk Corporation Catalytic oxidation of ammonia
EP0421468A1 (fr) * 1989-10-05 1991-04-10 Nkk Corporation Oxydation catalytique de l'ammoniac
WO1993020245A1 (fr) * 1992-03-27 1993-10-14 Still Otto Gmbh Procede combine de production de coke metallurgique et d'eponge de fer
EP0628621A3 (fr) * 1993-06-11 1995-02-15 Enviropower Oy Méthode et réacteur pour le traitement d'un gaz industriel.
US5562744A (en) * 1993-06-11 1996-10-08 Enviropower Oy Method for treating process gas
EP0629684A1 (fr) * 1993-06-17 1994-12-21 Texaco Development Corporation Procédé d'oxydation partielle pour produire un courant de gaz purifié chaud
EP0629685A1 (fr) * 1993-06-17 1994-12-21 Texaco Development Corporation Procédé d'oxydation partielle pour produire un courant de gaz purifié chaud
NL1001555C2 (nl) * 1995-10-27 1997-05-02 Biomass Technology Group B V Werkwijze voor de katalytische behandeling van een gasmengsel.
DE19907901C2 (de) * 1999-02-24 2001-11-29 Mg Technologies Ag Verfahren zur katalytischen Spaltung von flüchtigen höheren Kohlenwasserstoffen
KR200474985Y1 (ko) * 2008-09-26 2014-11-04 지멘스 브이에이아이 메탈스 테크놀로지스 게엠베하 건식 세정 및 건식 제거를 위한 시스템
WO2010034791A1 (fr) * 2008-09-26 2010-04-01 Siemens Vai Metals Technologies Gmbh & Co Procédé et dispositif de dépoussiérage et d'épuration à sec d'un gaz produit lors de la fabrication de fonte ou de gazéification de charbon
WO2010037465A1 (fr) * 2008-09-30 2010-04-08 Uhde Gmbh Epuration de gaz chaud
CN102164649A (zh) * 2008-09-30 2011-08-24 犹德有限公司 热气体净化
US8512444B2 (en) 2008-09-30 2013-08-20 Thyssenkrupp Uhde Gmbh Hot gas purification
RU2496555C2 (ru) * 2008-09-30 2013-10-27 Уде Гмбх Очистка горячего газа
CN102164649B (zh) * 2008-09-30 2014-02-26 犹德有限公司 热气体净化
AU2009300131B2 (en) * 2008-09-30 2014-07-17 Thyssenkrupp Uhde Gmbh Hot gas purification
TWI456044B (zh) * 2008-09-30 2014-10-11 Uhde Gmbh 熱氣處理方法
KR20110081186A (ko) * 2008-09-30 2011-07-13 우데 게엠베하 고온 가스 정제
WO2014183847A1 (fr) * 2013-05-16 2014-11-20 Ecoloop Gmbh Procédé de purification de gaz de synthèse

Also Published As

Publication number Publication date
ATE88210T1 (de) 1993-04-15
CA1335694C (fr) 1995-05-30
NO901393L (no) 1990-03-27
EP0310584A3 (en) 1990-03-14
JP2573681B2 (ja) 1997-01-22
LTIP1598A (en) 1995-08-25
NO901393D0 (no) 1990-03-27
SE8703816D0 (sv) 1987-10-02
DK175009B1 (da) 2004-04-19
SE459584B (sv) 1989-07-17
EP0310584B1 (fr) 1993-04-14
LT3842B (en) 1996-04-25
LV11188B (en) 1996-10-20
SE8703816L (sv) 1989-04-03
DK81090D0 (da) 1990-03-30
DK81090A (da) 1990-05-28
NO302422B1 (no) 1998-03-02
WO1989002909A1 (fr) 1989-04-06
DE3880253T2 (de) 1993-07-29
FI95924C (fi) 1996-04-10
FI95924B (fi) 1995-12-29
ES2039698T3 (es) 1993-10-01
AU2529788A (en) 1989-04-18
JPH03500420A (ja) 1991-01-31
GEP19980893B (en) 1998-04-10
LV11188A (lv) 1996-04-20
FI901613A0 (fi) 1990-03-30
AU612199B2 (en) 1991-07-04
DE3880253D1 (de) 1993-05-19

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