EP0310584B1 - Epuration de gaz brut - Google Patents

Epuration de gaz brut Download PDF

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Publication number
EP0310584B1
EP0310584B1 EP88850323A EP88850323A EP0310584B1 EP 0310584 B1 EP0310584 B1 EP 0310584B1 EP 88850323 A EP88850323 A EP 88850323A EP 88850323 A EP88850323 A EP 88850323A EP 0310584 B1 EP0310584 B1 EP 0310584B1
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EP
European Patent Office
Prior art keywords
gas
secondary stage
process according
active material
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.)
Expired - Lifetime
Application number
EP88850323A
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German (de)
English (en)
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EP0310584A2 (fr
EP0310584A3 (en
Inventor
Clas Ekström
Bengt-Göran Espenäs
Waclaw Kowalic
Erik Rensfelt
Lars Waldheim
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Studsvik Energiteknik AB
Original Assignee
TPS Termiska Processer AB
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Publication date
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Priority to AT88850323T priority Critical patent/ATE88210T1/de
Publication of EP0310584A2 publication Critical patent/EP0310584A2/fr
Publication of EP0310584A3 publication Critical patent/EP0310584A3/en
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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 refining 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 firing impossible, e.g. fireing of lime kilns or conversion of existing oil fired boilers.
  • Gasification of RDF with subsequent refining of the raw gas means an environmentally favourable method for energy recovery from wastes by utilization of refined gas in existing boilers or for cogeneration in diesel engines and/or 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. from peat) bound in tars, as well as ammonia, H2S (peat) or HCl (from RDF), furthermore give rise to emissions which are harmful to the environment (NO x , SO x and HCl, respectively, and chlorinated hydrocarbons, i.a. dioxines).
  • 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 raw gas to be used as a fuel gas, the raw gas containing tar and ammonia, in special cases also containing considerable quantities of hydrogen chloride, the raw 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 possibly absorbing) material.
  • a carbonaceous material e.g. bark, wood, peat or Refuse Derived Fuel, RDF
  • the process is characterized in that in order to reduce the gas contents of organic compounds in form of tar condensible at lower temperatures such as ambient temperatures, and of ammonia the refining is carried out in a secondary stage in the form of a fast circulating fluidized bed (CFB) having an upright reactor shaft, the bed material of which at least to a major part includes an active material in the form of a material that is catalytic for tar and ammonia conversion, consisting of a magnesium-calcium carbonate containing material, preferably dolomite, and/or the corresponding calcined (burnt) product, the particle size of the material being smaller than 2 mm, preferably smaller than 1 mm, while maintaining the operating temperature of the secondary stage within the interval of 600-1000°C, preferably within the interval of 700-900°C, the average suspension density in the reactor shaft within the interval of 80-250 kg/m3, the gas velocity in the reactor shaft calculated on an empty reactor shaft, below 10 m/s, preferably below 6 m/s, and
  • 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, in special cases to almost thermodynamic equilibrium.
  • 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 interest that these reactions become almost determined by the equilibrium and result
  • 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 can be 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 circulating 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 from 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 primary particle separator 27 preferably a U-beam separator of the same kind as the U-beam separator of the gasifier
  • a secondary separator 28 preferably a cyclone.
  • 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.
  • the almost dust-free gas 7, which leaves the dust removal stage 39, is fed to a scrubber 40, in which it is relieved from moisture and other water soluble components.
  • a scrubber 40 In the scrubber 40 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 secondary stage 25 has been integrated with a gasifier 3 based on CFB technology.
  • the gasifier 3 can produce the raw gas 2 from several different kinds of fuels, e.g. coarse bark, peat or refuse derived fuels RDF.
  • As bed material in the circulating bed of the gasifier 3 it is, as mentioned, convenient to use a catalytic and absorbing material of the same type as in the secondary stage 25.
  • 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)
  • Fats And Perfumes (AREA)
  • Transition And Organic Metals Composition Catalysts For Addition Polymerization (AREA)
  • Control And Other Processes For Unpacking Of Materials (AREA)
  • Artificial Filaments (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)

Claims (15)

  1. Un procédé de raffinage d'un gaz brut à utiliser comme gaz carburant et produit à partir d'une matière carbonée au moyen d'un processus de gazéification, dans lequel le raffinage est réalisé dans un étage secondaire séparée du processus de gazéification, caractérisé en ce que le raffinage est effectué, afin de réduire la teneur de gaz en composés organiques sous forme de goudron condensable à des températures plus basses comme des températures ambiantes, et en ammoniac, dans un étage secondaire en forme de lit fluidisé à circulation rapide pourvu d'une colonne de réacteur verticale, dont la matière de lit inclut au moins en majeure partie une matière active sous forme d'une matière qui est catalytique pour la conversion du goudron et de l'ammoniac, consistant en une matière contenant un carbonate de magnésium-calcium, de préférence de la dolomite, et/ou le produit correspondant calciné (brûlé), la dimension de particules de la matière étant inférieure à 2 mm, de préférence inférieure à 1 mm, en maintenant la température de fonctionnement de l'étage secondaire à l'intérieur de l'intervalle de 600° à 1000°C, de préférence à l'intérieur de l'intervalle de 700 à 900°C, la densité moyenne de suspension dans la colonne de réacteur étant dans l'intervalle de 80 à 250 kg/m³, la vitesse de gaz dans la colonne de réacteur de l'étage secondaire, calculée sur une colonne de réacteur vide, étant inférieure à 10 m/s, de préférence inférieure à 6 m/s, et le temps de résidence du gaz, calculé sur une colonne de réacteur vide, étant dans l'intervalle de 0,2 à 20 s, de préférence dans l'intervalle de 0,5 à 7 s, de façon à réaliser un contact entre le gaz qui passe et la matière active en vue d'une conversion catalytique du goudron et de l'ammoniac présents dans le gaz à des concentrations, dans le gaz raffiné, inférieures à 500 et 300 mg/Nm³ respectivement.
  2. Un procédé selon la revendication 1, dans lequel le gaz brut inclut du gaz chlorhydrique, caractérisé par une décharge intermittente ou continue de matière active contenant du gaz chlorhydrique absorbé à partir de l'étage secondaire et une alimentation intermittente ou continue d'une quantité correspondante de matière active fraîche à l'étage secondaire.
  3. Un procédé selon la revendication 1 ou 2, caractérisé par une addition simultanée de gaz oxydant, de préférence un gaz contenant de l'oxygène et/ou de la vapeur, au réacteur de l'étage secondaire.
  4. Un procédé selon l'une des revendications 1, 2 ou 3, caractérisé en ce que la température de fonctionnement de l'étage secondaire est réglée par des quantités additionnées de gaz contenant de l'oxygène.
  5. Un procédé selon l'une quelconque des revendications précédentes, caractérisé en ce qu'une matière active désactivée par suite d'un dépôt de carbone ou pour toutes autres raisons est déchargée de façon intermittente ou continue depuis l'étage secondaire et est remplacée par des quantités équivalentes de matière fraîche et/ou activée.
  6. Un procédé selon la revendication 5, caractérisé en ce que la matière active désactivée déchargés de l'étage secondaire est activée par un traitement à l'aide d'un gaz oxydant, de préférence un gaz contenant de l'oxygène et/ou de la vapeur, dans un étage d'activation séparé, la matière ainsi activée étant renvoyée à l'étage secondaire.
  7. Un procédé selon l'une quelconque des revendications précédentes, caractérisé en ce qu'une matière active désactivée par suite d'un dépôt de carbone ou pour toute autre raison est activée par traitement à l'aide d'un gaz oxydant, de préférence un gaz contenant de l'oxygène et/ou de la vapeur dans le système de recyclage de la matière de lit séparée de l'étage secondaire.
  8. Un processus selon la revendication 6 ou la revendication 7, caractérisé en ce que l'activation s'effectue à une température de fonctionnement située dans l'intervalle de 600 à 1000°C, de préférence dans l'intervalle de 750-900°C.
  9. Un procédé selon l'une quelconque des revendications 6, 7 ou 8, caractérisé en ce que la température de fonctionnement de l'activation est réglée au moyen de quantités ajoutées de gaz contenant de l'oxygène.
  10. Un procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que le gaz brut est amené directement du gazéificateur à l'étage secondaire sans aucun enlèvement intermédiaire de poussières.
  11. Un procédé selon la revendication 10, dans lequel le gazéificateur comprend un lit fluidisé à circulation rapide, caractérisé en ce que le gaz brut est amené directement du séparateur primaire du gazéificateur à l'étage secondaire.
  12. Un procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que le gaz fluidisant de l'étage secondaire comprend le gaz brut et éventuellement un gaz oxydant.
  13. Un procédé selon la revendication 12, caractérisé en ce que du gaz oxydant qui ne constitue pas un gaz fluidisant est ajouté au réacteur de l'étage secondaire à un ou plusieurs niveaux au-dessus de l'amenée de gaz fluidisant.
  14. Un procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que la teneur en gaz chlorhydrique dans le gaz raffiné qui quitte l'étage secondaire est encore abaissée au moyen d'une absorption sur la matière catalytique et absorbante restant dans le gaz après la séparation de particules de l'étage secondaire, le gaz étant d'abord refroidi après l'étage secondaire à une température considérablement plus basse, de préférence une température comprise entre 150 et 300°C, et étant ensuite soumis à une séparation additionnelle de poussière.
  15. Un procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que l'amenée de gaz brut à l'étage secondaire est reliée directement au séparateur primaire de particules d'un gazéificateur à lit fluidisé à circulation rapide, dans lequel la matière de lit en circulation consiste en une matière active du même type que dans l'étage secondaire, en ce que la poussière séparée dans l'étage secondaire, de préférence dans un séparateur secondaire de particules, est au moins partiellement recyclée vers la partie inférieure du réacteur de gazéification, et en ce qu'une matière de lit entraînée avec le gaz brut du gazéificateur et la matière éventuellement déchargée du bas du gazéificateur sont remplacées par la matière recyclée vers le réacteur de gazéification à partir de l'étage secondaire en combinaison avec de la matière fraîche catalytique et absorbante qui est ajoutée dans le gazéificateur de façon intermittente ou continue.
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 EP0310584A2 (fr) 1989-04-05
EP0310584A3 EP0310584A3 (en) 1990-03-14
EP0310584B1 true EP0310584B1 (fr) 1993-04-14

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Family Applications (1)

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EP88850323A Expired - Lifetime EP0310584B1 (fr) 1987-10-02 1988-09-28 Epuration de gaz brut

Country Status (15)

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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)

Families Citing this family (17)

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US5139756A (en) * 1989-10-05 1992-08-18 Nkk Corporation Catalytic oxidation of ammonia
JPH03122010A (ja) * 1989-10-05 1991-05-24 Nkk Corp アンモニアの接触酸化分解方法
US5827819A (en) * 1990-11-01 1998-10-27 Oregon Health Sciences University Covalent polar lipid conjugates with neurologically active compounds for targeting
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
DE4210003A1 (de) * 1992-03-27 1993-09-30 Ruhrkohle Ag Kombiniertes Verfahren zur Erzeugung von metallurgischem Koks und Eisenschwamm
FI96321C (fi) * 1993-06-11 1996-06-10 Enviropower Oy Menetelmä ja reaktori prosessikaasun käsittelemiseksi
US5403366A (en) * 1993-06-17 1995-04-04 Texaco Inc. Partial oxidation process for producing a stream of hot purified gas
US5401282A (en) * 1993-06-17 1995-03-28 Texaco Inc. Partial oxidation process for producing a stream of hot purified gas
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NO302422B1 (no) 1998-03-02
EP0310584A2 (fr) 1989-04-05
SE8703816L (sv) 1989-04-03
JP2573681B2 (ja) 1997-01-22
JPH03500420A (ja) 1991-01-31
WO1989002909A1 (fr) 1989-04-06
AU2529788A (en) 1989-04-18
DK81090A (da) 1990-05-28
NO901393L (no) 1990-03-27
FI95924B (fi) 1995-12-29
ES2039698T3 (es) 1993-10-01
NO901393D0 (no) 1990-03-27
DK175009B1 (da) 2004-04-19
GEP19980893B (en) 1998-04-10
CA1335694C (fr) 1995-05-30
DK81090D0 (da) 1990-03-30
AU612199B2 (en) 1991-07-04
ATE88210T1 (de) 1993-04-15
FI901613A0 (fi) 1990-03-30
LV11188B (en) 1996-10-20
SE8703816D0 (sv) 1987-10-02
LV11188A (lv) 1996-04-20
LTIP1598A (en) 1995-08-25
FI95924C (fi) 1996-04-10
EP0310584A3 (en) 1990-03-14
LT3842B (en) 1996-04-25
DE3880253D1 (de) 1993-05-19
SE459584B (sv) 1989-07-17
DE3880253T2 (de) 1993-07-29

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