EP1165727B1 - Method and process for cleaning a productgas of a gasification reactor - Google Patents

Method and process for cleaning a productgas of a gasification reactor Download PDF

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Publication number
EP1165727B1
EP1165727B1 EP00976089A EP00976089A EP1165727B1 EP 1165727 B1 EP1165727 B1 EP 1165727B1 EP 00976089 A EP00976089 A EP 00976089A EP 00976089 A EP00976089 A EP 00976089A EP 1165727 B1 EP1165727 B1 EP 1165727B1
Authority
EP
European Patent Office
Prior art keywords
reactor
productgas
zone
gas
bed
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
EP00976089A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP1165727A1 (en
Inventor
Esa Kurkela
Pekka Stahlberg
Pekka Simell
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.)
Valtion Teknillinen Tutkimuskeskus
Original Assignee
Valtion Teknillinen Tutkimuskeskus
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Publication date
Application filed by Valtion Teknillinen Tutkimuskeskus filed Critical Valtion Teknillinen Tutkimuskeskus
Publication of EP1165727A1 publication Critical patent/EP1165727A1/en
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Publication of EP1165727B1 publication Critical patent/EP1165727B1/en
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Classifications

    • 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
    • C10K1/34—Purifying combustible gases containing carbon monoxide by catalytic conversion of impurities to more readily removable materials
    • 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
    • C10K3/001—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 thermal treatment
    • C10K3/003—Reducing the tar content
    • C10K3/008—Reducing the tar content by cracking
    • 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

Definitions

  • the invention relates to a method for cleaning a productgas of a gasification reactor of tars and other organic compounds that condense out of the gas while it cools in a fluidized bed reactor acting as cracker.
  • the invention relates also to equipment for carrying out the method.
  • a catalyzed technique for purifying gas has been an object of research for many years. According to familiar techniques prevention of the formation of tar and efficient decomposition of tars may be accomplished in three alternate ways:
  • the first alternative requires, however, in practice gasification temperatures of more than from 900°C to 950°C this being not feasible with each and every fuel. Also, it has been noted that in the gasification reactor itself it is difficult to reach tar contents of less than 2-4 g/m 3 n because the contact between the gas and the catalytically active material is not good enough. Thus, in many applications a separate secondary cracking is required. According to research done by the applicant a complete decomposition of tarry compounds may be accomplished in principle with both nickel-based and calcium-based catalysts. However, a drawback of the nickel-based catalysts is the high prize of the material, its toxicity as well as difficulties relating to realizing equipment run-ups and run-downs. Furthermore the lifetime of such catalysts is so far not known.
  • lime-based catalysts that is the use of limestone and/or dolomite
  • full conversion of tars has been reached in a fixed bed reactor already with a very short residence time (less than 0.5 s) and a moderate temperature of 850-900°C.
  • the contact between the tar-containing gas and the bed material is ideal, but the reactor is, however, extremely vulnerable to clogging caused by dust and finely divided limestone and is therefore not applicable to industrial use.
  • Patent Publication SE 8,703,816 a solution is put forward that applies a separate moving bed catalysis reactor with which reasonably good results have been obtained.
  • a moving bed reactor is large and expensive and calcium-containing bed materials are ground there very fast due to the high flow rate (typically about 5 m/s). In practice this leads to high consumption of limestone.
  • an objective of the invention is to develop a method for purifying the productgas of a gasification reactor of tars and of other organic compounds condensing out of the gas while it cools in a cracker reactor, which method solves the problems mentioned above and meets the following demands: a) the contact between the gas and the catalyst is efficient, b) the method is not sensitive to clogging by dust and c) the method can be realized on industrial scale with costs low enough.
  • the inventive method is characterized in that the cleaning is accomplished in a spouted-bed reactor, where
  • the productgas leaving the gasifier is introduced into a secondary cracker reactor, the bottom part of which functions by spouted bed principle and the upper part of which functions as an equalizing and separation space.
  • a spouted bed reactor is a technique known to one skilled in the art per se from other applications.
  • a forth or fluidized bed zone that functions as a traditional fluidized bed.
  • the operation temperature needed for cracking of tars - 700-1200°C, preferably 800-1000°C - is reached by regulating the inlet of the fluidization gas of the bubbling fluidized bed.
  • the bed material in the first and/or the forth zone may comprise limestone, dolomite, sand or a mixture of at least two of these depending on the residual tar level aimed at.
  • the productgas to be purified is fed into the reactor by a rate that is 15-50 m/s, preferably 20-45 m/s.
  • the flow rate of the gas flow is yet again 0.1-1.2 m/s, preferably 0.3-1.0 m/s.
  • the fluidized bed of the first zone is bubbled with the aid of an oxidizing gas which gas is fed into the reactor at a rate that is 0.4-2.0 m/s, preferably 0.5-1.5 m/s.
  • Said oxidizing gas may be air, oxygen, water vapor or a mixture of at least two of these.
  • said oxidizing gas is fed into the reactor through a distributor plate.
  • the productgas to be cleansed by the inventive method may be for example a gasification product of charcoal, peat, solid biomass or waste-based recirculated fuel.
  • a further object of the invention is an equipment for carrying out the inventive method, which equipment is characterized in that it comprises
  • the reactor comprises additionally a second cylindrical part that is arranged above the conical part.
  • a productgas to be purified is introduced to the reactor through an inlet tube situated in the bottom part of the reactor which inlet tube is placed inside a larger outer tube.
  • the oxidizing gas needed for cracking and used for partial combustion is introduced through the distributor plate in the space between the inlet tube and the outer tube.
  • the tubes are dimensioned such that in this intervening space used for introduction of oxidizing gas reins a flow rate that is beneficial from the point of view of functioning of the bubbling fluidized bed (typically 0.5-1.5 m/s).
  • the surface height in the reactor may be adjusted according to the tar removal degree desired on a higher or lower level. As its lowest the reactor comprises only the spouted zone and above that an equalizing zone from which the particles swept away with the gas are returned back below.
  • the upper part of the reactor is dimensioned such that it functions as a separator for the bed particles swept away with the spout (flow rate is typically about 0.3-1 m/s).
  • flow rate is typically about 0.3-1 m/s.
  • the equipment may be used even in large cracking reactors whereby there are more inlet tubes and they are essentially parallel to each other. This kind of application is described more in detail below.
  • particles contained in the productgas don't cause problems such as in traditional fluidized bed crackers equipped with a distributor plate and the fluidization produced by an oxidizing gas stabilizes the spouted bed function such that an even functioning is attained with widely varying inlet flow rates of the productgas (even below 20 m/s) and with bed materials of varying particle sizes.
  • fluidization with an oxidizing gas carries likewise part of the pressure drop caused by fluidization of bed material, thanks to which the pressure of the incoming productgas is lower, which is desirable in order to prevent leaks of feed equipment and other openings.
  • the incoming oxidizing gas is very efficiently mixed with the productgas because bed material particles thrown upwards by the gas spout return back downwards along the conical walls directly into the incoming air flow to be drawn from it again back into the upwardly mobile spout.
  • inventive method and equipment comprise suitability of the space situated beneath the conical upper part and fluidized with the oxidizing gas even to removal of used bed material when it is necessary to change bed material for example due to poisoning due to reaction between HCl and limestone or for example due to agglomeration.
  • Fig. 1 presents an equipment according to the first embodiment of the invention in side-view.
  • the equipment 1 comprises an inlet tube 3 for a productgas 2, a bubbling fluidized bed 5 arranged beneath an inlet opening 4.
  • the fluidized bed 5 is bubbled by introducing air 6 through a distributor plate 7.
  • Bed material particles 9 thrown upwards by gas spout 8 formed by productgas 2 are returned back downwards along the conical walls 10 directly into the incoming flow of air to be drawn from it again back into the upwardly mobile spout 8.
  • the drawing presents an outlet channel 13 for purified gas 12 as well as an outlet channel 14 for the bed material of fluidized bed 5.
  • Fig. 2a there is presented a part of an equipment according to the second embodiment of the invention in side-view.
  • the equipment 15 is larger than the one presented in Fig. 1, and it comprises an inlet channel 3 for productgas 2 that is divided to multiple feed channels of which the side-view presented here comprises three, 3a, 3b and 3c. Additionally, the drawing presents introduction of air 6 through a distributor plate 7 as well as a bubbling fluidized bed 5.
  • Fig. 2a allows for an efficient mixing and a controlled fluidization even in a large sized cracker in which good results are not obtained by using only one large inlet tube.
  • introduction of gas is divided to several smaller tubes that are placed inside the same space fluidized by air even in large crackers as efficient a mixing is obtained as in a small cracker in addition to which the plunging of bed material into the inlet tube typical of spouted-bed reactors is avoided.
  • FIG. 2b there is presented a cross-sectional view AA of the equipment featured in Fig. 2a.
  • inlet tubes for gas 3a-3i and the holes 16 in distributor plate 7 are illustrated.
  • the holes 16 may be situated according to desires.
  • the inventive equipment has also been tested in a bench-scale sized cracker, the diameter of the upper part of which was about 100 mm and that was connected to a fluidized bed gasifier.
  • inventive cracker are not limited to the purification of productgas of fluidized bed gasification presented in the example but rather the method may be applied, for example, even to treatment of gases formed in fixed bed gasifiers or in other processes.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Industrial Gases (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Cleaning In General (AREA)
  • Processing Of Solid Wastes (AREA)
EP00976089A 1999-11-04 2000-11-03 Method and process for cleaning a productgas of a gasification reactor Expired - Lifetime EP1165727B1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FI992381A FI107164B (fi) 1999-11-04 1999-11-04 Menetelmä ja laitteisto kaasutusreaktorin tuotekaasun puhdistamiseksi
FI992381 1999-11-04
PCT/FI2000/000960 WO2001032808A1 (en) 1999-11-04 2000-11-03 Method and process for cleaning a productgas of a gasification reactor

Publications (2)

Publication Number Publication Date
EP1165727A1 EP1165727A1 (en) 2002-01-02
EP1165727B1 true EP1165727B1 (en) 2005-10-26

Family

ID=8555557

Family Applications (1)

Application Number Title Priority Date Filing Date
EP00976089A Expired - Lifetime EP1165727B1 (en) 1999-11-04 2000-11-03 Method and process for cleaning a productgas of a gasification reactor

Country Status (8)

Country Link
EP (1) EP1165727B1 (es)
AT (1) ATE307862T1 (es)
AU (1) AU1398101A (es)
DE (1) DE60023468T2 (es)
DK (1) DK1165727T3 (es)
ES (1) ES2250212T3 (es)
FI (1) FI107164B (es)
WO (1) WO2001032808A1 (es)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10995274B2 (en) 2015-07-21 2021-05-04 British Columbia Biocarbon Ltd. Biocoal fuel product and processes and systems for the production thereof

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100427199C (zh) * 2006-01-20 2008-10-22 哈尔滨工业大学 锥形无壁效应反应器
US8191703B2 (en) 2010-02-18 2012-06-05 Ecolab Usa Inc. Conveyor system monitoring and maintenance
CN109679698A (zh) * 2019-01-23 2019-04-26 江苏普格机械有限公司 中心射流管及采用该中心射流管的流化床煤气化炉

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5213587A (en) * 1987-10-02 1993-05-25 Studsvik Ab Refining of raw gas
US4865625A (en) * 1988-05-02 1989-09-12 Battelle Memorial Institute Method of producing pyrolysis gases from carbon-containing materials
DE4023060A1 (de) * 1990-07-20 1992-01-23 Metallgesellschaft Ag Verfahren zur kuehlung von heissen prozessgasen
FI93274C (fi) * 1993-06-23 1995-03-10 Ahlstroem Oy Menetelmä ja laite kuuman kaasuvirran käsittelemiseksi tai hyödyntämiseksi
FI97424C (fi) * 1993-06-23 1996-12-10 Foster Wheeler Energia Oy Menetelmä ja laite kuuman kaasun käsittelemiseksi tai hyödyntämiseksi

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10995274B2 (en) 2015-07-21 2021-05-04 British Columbia Biocarbon Ltd. Biocoal fuel product and processes and systems for the production thereof

Also Published As

Publication number Publication date
FI107164B (fi) 2001-06-15
EP1165727A1 (en) 2002-01-02
ES2250212T3 (es) 2006-04-16
DK1165727T3 (da) 2006-03-06
DE60023468T2 (de) 2006-07-27
WO2001032808A1 (en) 2001-05-10
DE60023468D1 (de) 2005-12-01
ATE307862T1 (de) 2005-11-15
AU1398101A (en) 2001-05-14

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