EP0310584A2 - Reinigung von Rohgas - Google Patents
Reinigung von Rohgas Download PDFInfo
- 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
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Images
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)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
- Gas Separation By Absorption (AREA)
- Artificial Filaments (AREA)
- Transition And Organic Metals Composition Catalysts For Addition Polymerization (AREA)
- Fats And Perfumes (AREA)
- Control And Other Processes For Unpacking Of Materials (AREA)
- Carbon And Carbon Compounds (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
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 |
---|---|---|---|
SE8703816A SE459584B (sv) | 1987-10-02 | 1987-10-02 | Foerfarande foer foeraedling av raagas framstaelld ur ett kolhaltigt material |
SE8703816 | 1987-10-02 |
Publications (3)
Publication Number | Publication Date |
---|---|
EP0310584A2 true EP0310584A2 (de) | 1989-04-05 |
EP0310584A3 EP0310584A3 (en) | 1990-03-14 |
EP0310584B1 EP0310584B1 (de) | 1993-04-14 |
Family
ID=20369746
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP88850323A Expired - Lifetime EP0310584B1 (de) | 1987-10-02 | 1988-09-28 | Reinigung von Rohgas |
Country Status (15)
Country | Link |
---|---|
EP (1) | EP0310584B1 (de) |
JP (1) | JP2573681B2 (de) |
AT (1) | ATE88210T1 (de) |
AU (1) | AU612199B2 (de) |
CA (1) | CA1335694C (de) |
DE (1) | DE3880253T2 (de) |
DK (1) | DK175009B1 (de) |
ES (1) | ES2039698T3 (de) |
FI (1) | FI95924C (de) |
GE (1) | GEP19980893B (de) |
LT (1) | LT3842B (de) |
LV (1) | LV11188B (de) |
NO (1) | NO302422B1 (de) |
SE (1) | SE459584B (de) |
WO (1) | WO1989002909A1 (de) |
Cited By (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0421468A1 (de) * | 1989-10-05 | 1991-04-10 | Nkk Corporation | Katalytische Oxidation von Ammoniak |
US5139756A (en) * | 1989-10-05 | 1992-08-18 | Nkk Corporation | Catalytic oxidation of ammonia |
WO1993020245A1 (de) * | 1992-03-27 | 1993-10-14 | Still Otto Gmbh | Kombiniertes verfahren zur erzeugung von metallurgischem koks und eisenschwamm |
EP0628621A2 (de) * | 1993-06-11 | 1994-12-14 | Enviropower Oy | Methode und Reaktor zur Behandlung von einem Prozessgas |
EP0629684A1 (de) * | 1993-06-17 | 1994-12-21 | Texaco Development Corporation | Teiloxydationsverfahren zur Herstellung eines Stromes von heissem gereinigten Gas |
EP0629685A1 (de) * | 1993-06-17 | 1994-12-21 | Texaco Development Corporation | Teiloxydationsverfahren zur Herstellung eines Stromes von heissem gereinigten Gas |
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 (de) * | 2008-09-26 | 2010-04-01 | Siemens Vai Metals Technologies Gmbh & Co | Verfahren und vorrichtung zur trockenen entstaubung und reinigung von bei der eisenerzeugung oder kohlevergasung produziertem gas |
WO2010037465A1 (de) * | 2008-09-30 | 2010-04-08 | Uhde Gmbh | Heissgasreinigung |
WO2014183847A1 (de) * | 2013-05-16 | 2014-11-20 | Ecoloop Gmbh | Verfahren zur reinigung von synthesegasen |
Families Citing this family (6)
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 |
US10011792B2 (en) | 2010-08-16 | 2018-07-03 | Nikhil Manubhai Patel | Sandwich gasification process for high-efficiency conversion of carbonaceous fuels to clean syngas with zero residual carbon discharge |
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 |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3807090A (en) * | 1970-12-02 | 1974-04-30 | Exxon Research Engineering Co | Purifications of fuels |
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 |
GB2180849A (en) * | 1985-09-25 | 1987-04-08 | Skf Steel Eng Ab | Producing clean gas containing hydrogen and carbon monoxide |
FR2594140A1 (fr) * | 1986-02-13 | 1987-08-14 | Goetaverken Energy Syst Ab | Procede pour eliminer des substances indesirables d'un gaz qui est produit par gazeification pyrolytique |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2824534A1 (de) * | 1977-06-03 | 1978-12-07 | Hitachi Ltd | Verfahren zur reinigung von schwefelwasserstoff und ammoniak enthaltenden heissen gasen |
DE3017998C2 (de) * | 1980-05-10 | 1994-05-26 | Krupp Koppers Gmbh | Verfahren zur katalytischen Behandlung von Partialoxidationsrohgas |
DE3716199A1 (de) | 1987-05-14 | 1988-11-24 | Linde Ag | Verfahren und vorrichtung zur reinigung von rohgasen unter gleichzeitiger gewinnung von synthese- und brenngas |
-
1987
- 1987-10-02 SE SE8703816A patent/SE459584B/sv not_active Application Discontinuation
-
1988
- 1988-09-28 GE GEAP19881491A patent/GEP19980893B/en unknown
- 1988-09-28 AT AT88850323T patent/ATE88210T1/de not_active IP Right Cessation
- 1988-09-28 JP JP63508056A patent/JP2573681B2/ja not_active Expired - Fee Related
- 1988-09-28 WO PCT/SE1988/000502 patent/WO1989002909A1/en active IP Right Grant
- 1988-09-28 AU AU25297/88A patent/AU612199B2/en not_active Ceased
- 1988-09-28 DE DE8888850323T patent/DE3880253T2/de not_active Expired - Fee Related
- 1988-09-28 ES ES198888850323T patent/ES2039698T3/es not_active Expired - Lifetime
- 1988-09-28 EP EP88850323A patent/EP0310584B1/de not_active Expired - Lifetime
- 1988-09-30 CA CA000579047A patent/CA1335694C/en not_active Expired - Fee Related
-
1990
- 1990-03-27 NO NO901393A patent/NO302422B1/no not_active IP Right Cessation
- 1990-03-30 DK DK199000810A patent/DK175009B1/da not_active IP Right Cessation
- 1990-03-30 FI FI901613A patent/FI95924C/fi not_active IP Right Cessation
-
1993
- 1993-10-25 LV LVP-93-1170A patent/LV11188B/en unknown
- 1993-12-15 LT LTIP1598A patent/LT3842B/lt not_active IP Right Cessation
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3807090A (en) * | 1970-12-02 | 1974-04-30 | Exxon Research Engineering Co | Purifications of fuels |
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 |
GB2180849A (en) * | 1985-09-25 | 1987-04-08 | Skf Steel Eng Ab | Producing clean gas containing hydrogen and carbon monoxide |
FR2594140A1 (fr) * | 1986-02-13 | 1987-08-14 | Goetaverken Energy Syst Ab | Procede pour eliminer des substances indesirables d'un gaz qui est produit par gazeification pyrolytique |
Cited By (21)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0421468A1 (de) * | 1989-10-05 | 1991-04-10 | Nkk Corporation | Katalytische Oxidation von Ammoniak |
US5139756A (en) * | 1989-10-05 | 1992-08-18 | Nkk Corporation | Catalytic oxidation of ammonia |
WO1993020245A1 (de) * | 1992-03-27 | 1993-10-14 | Still Otto Gmbh | Kombiniertes verfahren zur erzeugung von metallurgischem koks und eisenschwamm |
EP0628621A2 (de) * | 1993-06-11 | 1994-12-14 | Enviropower Oy | Methode und Reaktor zur Behandlung von einem Prozessgas |
EP0628621A3 (de) * | 1993-06-11 | 1995-02-15 | Enviropower Oy | Methode und Reaktor zur Behandlung von einem Prozessgas. |
US5562744A (en) * | 1993-06-11 | 1996-10-08 | Enviropower Oy | Method for treating process gas |
EP0629684A1 (de) * | 1993-06-17 | 1994-12-21 | Texaco Development Corporation | Teiloxydationsverfahren zur Herstellung eines Stromes von heissem gereinigten Gas |
EP0629685A1 (de) * | 1993-06-17 | 1994-12-21 | Texaco Development Corporation | Teiloxydationsverfahren zur Herstellung eines Stromes von heissem gereinigten Gas |
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 (de) * | 2008-09-26 | 2010-04-01 | Siemens Vai Metals Technologies Gmbh & Co | Verfahren und vorrichtung zur trockenen entstaubung und reinigung von bei der eisenerzeugung oder kohlevergasung produziertem gas |
KR200474985Y1 (ko) * | 2008-09-26 | 2014-11-04 | 지멘스 브이에이아이 메탈스 테크놀로지스 게엠베하 | 건식 세정 및 건식 제거를 위한 시스템 |
WO2010037465A1 (de) * | 2008-09-30 | 2010-04-08 | Uhde Gmbh | Heissgasreinigung |
KR20110081186A (ko) * | 2008-09-30 | 2011-07-13 | 우데 게엠베하 | 고온 가스 정제 |
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 |
WO2014183847A1 (de) * | 2013-05-16 | 2014-11-20 | Ecoloop Gmbh | Verfahren zur reinigung von synthesegasen |
Also Published As
Publication number | Publication date |
---|---|
LTIP1598A (en) | 1995-08-25 |
LV11188A (lv) | 1996-04-20 |
FI901613A0 (fi) | 1990-03-30 |
FI95924B (fi) | 1995-12-29 |
EP0310584A3 (en) | 1990-03-14 |
NO901393L (no) | 1990-03-27 |
JP2573681B2 (ja) | 1997-01-22 |
FI95924C (fi) | 1996-04-10 |
WO1989002909A1 (en) | 1989-04-06 |
DE3880253T2 (de) | 1993-07-29 |
AU2529788A (en) | 1989-04-18 |
DE3880253D1 (de) | 1993-05-19 |
ATE88210T1 (de) | 1993-04-15 |
LT3842B (en) | 1996-04-25 |
ES2039698T3 (es) | 1993-10-01 |
NO901393D0 (no) | 1990-03-27 |
CA1335694C (en) | 1995-05-30 |
EP0310584B1 (de) | 1993-04-14 |
DK81090A (da) | 1990-05-28 |
AU612199B2 (en) | 1991-07-04 |
DK175009B1 (da) | 2004-04-19 |
JPH03500420A (ja) | 1991-01-31 |
LV11188B (en) | 1996-10-20 |
SE8703816L (sv) | 1989-04-03 |
NO302422B1 (no) | 1998-03-02 |
SE8703816D0 (sv) | 1987-10-02 |
DK81090D0 (da) | 1990-03-30 |
SE459584B (sv) | 1989-07-17 |
GEP19980893B (en) | 1998-04-10 |
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