EP1224246B1 - Verfahren zur entfernung von festschlacken aus einem wässrigen gemisch - Google Patents

Verfahren zur entfernung von festschlacken aus einem wässrigen gemisch Download PDF

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Publication number
EP1224246B1
EP1224246B1 EP00969277A EP00969277A EP1224246B1 EP 1224246 B1 EP1224246 B1 EP 1224246B1 EP 00969277 A EP00969277 A EP 00969277A EP 00969277 A EP00969277 A EP 00969277A EP 1224246 B1 EP1224246 B1 EP 1224246B1
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EP
European Patent Office
Prior art keywords
vessel
slag
water
slag particles
process according
Prior art date
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Application number
EP00969277A
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English (en)
French (fr)
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EP1224246A1 (de
Inventor
Isaac Cornelis Van Den Born
Johannes Gerardus Maria Schilder
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Shell Internationale Research Maatschappij BV
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Shell Internationale Research Maatschappij BV
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/52—Ash-removing devices
    • 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
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment

Definitions

  • the present invention is directed to a process to remove solid slag from a mixture of solid slag and water present in a quench zone, which quench zone is part of a process for the preparation of synthesis gas by partial combustion of finely dispersed solid carbon-containing fuel with an oxygen-containing gas.
  • GB-A-2086931 discloses a process for ash removal and synthesis gas generation from coal.
  • a problem of this sluicing procedure is that, when the valve between the lockhopper and the quench vessel is closed, the slag accumulating up-stream this valve has a tendency for bridging at the narrow space just above the said valve. It has appeared very difficult to have the slag to fall into the lockhopper after reconnecting the lockhopper to the gasification system.
  • This problem is solved by the process disclosed in EP-A-290087, wherein a permanent nitrogen-gas bubble or nitrogen-gas cap is maintained in the lockhopper.
  • One disadvantage is the need to install additional equipment to supply nitrogen and the associated costs of the nitrogen consumption during every sluicing cycle.
  • a further disadvantage is that together with the discharged mixture an amount of sulphur compounds, of which hydrogen sulphide is the most prominent, and other dissolved components, for example ammonia, chloride and carbon monoxide, are also discharged.
  • Hydrogen sulphide is formed in the reactor from sulphur containing compounds which are present in the hydrocarbon feed. Part of the hydrogen sulphide will dissolve in the water present in the slag quench vessel and will thus be discharged together with the slag in the above described process.
  • the object of the present invention is a simple process to quickly separate solid slag particles from a quench zone, containing a mixture of said slag particles and water, such that no or very little sulphur containing compounds are being removed with the slag from the quench zone.
  • the present process is directed to separate slag particles from a process for the preparation of synthesis gas by partial combustion of finely dispersed solid carbon-containing fuel with an oxygen-containing gas.
  • carbon-containing fuel are coal, peat, wood, coke, for example petroleum coke, soot, carbon containing waste, biomass and mixtures of these. Mixtures of the aforementioned feedstocks and metal containing waste streams can also be used as feed.
  • the ratio of volume of water poor in slag, which is extracted from the second vessel, relative to the volume of solids passing conduit from the first vessel to the second vessel in the same time period is preferably between 0.7 and 1.5 and more preferably between 0.8 and 1.
  • the volume of liquid extracted from the second vessel and supplied to the first vessel is about the same as the volume of solids passing from the first to the second vessel due to gravity.
  • the liquid in the connecting conduit between first and second vessel will then be kept close to stagnant. This situation further reduces any sulphur compounds from entering the second vessel.
  • the mass flux of the slag particles in the connecting conduit between the first and second vessel is between 100-150 kg slag particles per square meter of the cross sectional area of the conduit or valve, whatever the smallest, per second (kg/m 2 /s).
  • a gradient in the concentration of sulphur compounds will be present, wherein the concentration of sulphur compounds in the first vessel will be lower than in the quench zone.
  • This concentration gradient is especially achieved when the height over diameter ratio of the first vessel is greater than three.
  • the water poor in slag extracted from the second vessel is fed to the lower end of the first vessel to further increase this concentration gradient. This concentration gradient is advantageous because it further reduces the chances of any sulphur compounds entering the second vessel.
  • the volume of the first vessel is preferably of the same size or larger than the second vessel.
  • the additional volume acts as buffer capacity for problem solving and in addition reduces the chances of any sulphur compounds entering the second vessel.
  • When closing the first vessel from the second vessel in step (c) preferable no or very few slag particles will be present in the connecting conduit, thereby reducing the chance that slag particles obstruct the valve present in said conduit, thereby reducing the change on damaging the valve, and keeping the buffer capacity available to anticipate for problems that may rise.
  • the second vessel is preferably not too small because this will result in a too high sluicing frequency, resulting in a poor capacity of the process.
  • the volume of the first vessel is between 2 and 3 times the volume of the second vessel.
  • the volume of the second vessel will be determined by the required capacity to remove slag particles.
  • One skilled in the art can easily determine the optimal volume taken into account the required time to conduct steps (a)-(e) and the desire to minimise the size of the vessels.
  • step (d) In order to further reduce the amount of sulphur compounds which can be discharged from the first vessel to the second vessel it is advantageous to fill the second vessel with clean or fresh water after the slag particles are removed from the second vessel in step (d) and/or in step (e) before performing step (a).
  • slag particles enter the second vessel part of this clean water having suitably about the volume of the entering particles, is discharged to the first vessel, or alternatively, but less preferred, to another outlet.
  • this clean water enters the first vessel a further reduction in this first vessel of the content of sulphur compounds results as also discussed above.
  • the first vessel is also provided with means to discharge water poor in slag.
  • This water can advantageously be used as medium to cool the quench zone by extracting heat form this stream against cooling water, cooling air or another medium. Also it may be advantageously to use this water to destroy and/or clean deposits formed on the surface of the water layer present in the quench zone and deposits present on the quench zone construction itself. It may be advantageous to bleed some of this stream to prevent building up of contaminants.
  • the preferred position at which the water poor in slag is discharged from the first vessel is the same as discussed for the second vessel.
  • the present process is very advantageous to be used in a situation wherein the pressure in the first vessel is higher than the pressure of the environment into which the separated solids are discharged to from the second vessel.
  • the pressure in the quench zone and the associated first vessel in the process according the invention is typically between 20 and 60 bars, while the solids are normally discharged at about ambient pressure from the second vessel, sometimes referred to as lockhopper vessel.
  • the Figure represents an apparatus for performing the above described preferred embodiment of the process according to the present invention.
  • the apparatus comprises a first vessel (1), a second vessel (2), preferably positioned below the first vessel, and a first (3) and second (4) conduit fluidly connecting the first and second vessel.
  • the first conduit (3) is preferably located such that slag particles in step (b) can move by gravity from the first vessel (1) to the second vessel (2).
  • Second conduit (4) is provided with pumping means (5) to transport water poor in slag particles from the second vessel to the first vessel.
  • Suitable means to pump a liquid are for example a gear pump, a lobe pump, a rotary pump, a centrifugal pump or a riser.
  • the inlet of second conduit (4) is located such that water which is poor in slag particles is pumped from the second vessel (2) into the first vessel (1). Slag particles entering second vessel (2) via conduit (3) will accumulate in the lower part of the second vessel resulting in that the upper part of the second vessel is poor in slag particles relative to the lower part.
  • the inlet (6) of conduit (4) is therefore located in the upper part of the second vessel (2) and away from the outlet opening (8) of the first conduit (3) entering the second vessel (2). More preferably a tubular shield (7) is present around the outlet (8) of conduit (3) which directs the slag particles entering the second vessel (2) downwards and away from the inlet (6) of the second conduit (4).
  • the second vessel is furthermore provided with an outlet opening (9) through which solid particles can be discharged and the first vessel is provided with an inlet opening (10) for receiving the mixture from the quench zone (14).
  • the opening (10) may optionally be provided with a slag grinder to break large slag particles before entering the first vessel. If no slag grinder is present the opening (10) will typically be larger than the opening in the conduit connecting the first (1) and second (2) vessel, thereby enabling a trouble free flow of slag particles into the first vessel (1) from the quench zone (14).
  • valve (11) is closed and pump (5) is stopped.
  • valve (13) is in a open position to discharge the slag particles from the second vessel (2).
  • the Figure also shows a discharge zone (12).
  • the Figure also shows a conduit (15) through which water poor in slag can be removed from the first vessel and a tubular shield (16) which has the same functionality as shield (7) described in the second vessel.
  • vessel 1 was loaded with a mixture of water and 172 kg slag obtained from a coal gasification process having a density of 2335 kg/m 3 . Most slag particles were present at the bottom of vessel 1 near valve 11. Vessel 2 was loaded with clean water. After opening of valve 11, having a diameter of 10 cm, and after start-up of pump 5 a stable sluicing flow through the valve was observed. The pump flow rate was 15.5 litre/minute and the 172 kg of slag was sluiced out in 3.65 minutes. The ratio of volume of liquid which is transported from the second vessel to the first vessel via conduit (4) relative to the volume of solids passing conduit (3) in the same time period is in this example thus 0.75.
  • Example 1 was repeated except that the pump flow was 36.3 litre/minute. The same 172 kg of slag was sluiced out in 2.44 minutes. The ratio of volume of liquid which is transported from the second vessel to the first vessel via conduit (4) relative to the volume of solids passing conduit (3) in the same time period is in this example 1.18.
  • Example 1 was repeated except that pump 5 was not used.
  • the flow through valve 11 was very unstable and the experiment was repeated 15 times in order to obtain a reliable test result. On average it took the 172 kg of slag 5.6 minutes to pass valve 11.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)
  • Gasification And Melting Of Waste (AREA)

Claims (10)

  1. Verfahren zur Entfernung von festen Schlacketeilchen aus einem Gemisch von festen Schlacketeilchen und Wasser, welches Gemisch in einer Abschreckzone vorliegt, welche Abschreckzone Teil eines Verfahren der Herstellung von Synthesegas durch teilweise Verbrennung von feinverteilten festen Kohlenstoff-enthaltendem Brennstoff mit einem sauerstoffhältigen Gas ist, durch
    (a) Abführen des Gemisches aus der Abschreckzone in ein erstes Gefäß
    (b) Abführen von Schlacketeilchen aus dem ersten Gefäß in ein zweites Gefäß mittels Schwerkraft, welches zweite Gefäß unterhalb des ersten Gefäßes angeordnet und mit diesem mittels einer offenen verbindenden Leitung fluidverbunden und ferner mit geschlossenen Mitteln zum Abführen der Schlacke aus seinem unteren Ende ausgestattet ist, und Abführen von an fester Schlacke armem Wasser aus dem zweiten Gefäß über eine Leitung, die mit Pumpmitteln ausgestattet ist und einen Einlaß aufweist, welcher derart angeordnet ist, daß an Schlacketeilchen armes Wasser aus dem zweiten Gefäß gepumpt wird,
    (c) fluidmäßiges Abschließen des ersten Gefäßes vom zweiten Gefäß
    (d) Öffnen der Mittel zum Abführen von Schlacke aus dem zweiten Gefäß, um Schlacke aus dem zweiten Gefäß in eine einen niedrigeren Druck aufweisende Zone zu entfernen, und
    (e) Schließen der Mittel zum Abführen der Schlacke aus dem zweiten Gefäß und Wiederholen der Schritte (a) bis (e).
  2. Verfahren nach Anspruch 1, worin das im Schritt (b) erhaltene an Schlacke arme Wasser dem ersten Gefäß zugeführt wird.
  3. Verfahren nach Anspruch 2, worin das an Schlacke arme Wasser zum unteren Ende eines ersten Gefäßes zugeführt wird, welches erste Gefäß ein Höhe-zu-DurchmesserVerhältnis von mehr als 3 aufweist.
  4. Verfahren nach einem der Ansprüche 1 bis 3, worin das an Feststoffen arme Wasser aus dem oberen Teil des zweiten Gefäßes an einer Stelle abgeführt wird, welche von der Auslaßöffnung der ersten Leitung, die in das zweite Gefäß eintritt, entfernt ist.
  5. Verfahren nach Anspruch 4, worin eine röhrenförmige Abschirmung um die Auslaßöffnung der ersten Leitung vorhanden ist, welche die in das zweite Gefäß eintretenden Schlacketeilchen nach unten und weg vom Einlaß der Leitung, durch welche an Schlacketeilchen armes Wasser aus dem zweiten Gefäß gepumpt wird, steuert.
  6. Verfahren nach einem der Ansprüche 1 bis 5, worin das Verhältnis des Volumens an Wasser, welches aus dem zweiten Gefäß extrahiert wird, relativ zum Volumen an festen Schlacketeilchen, welche in der gleichen Zeitspanne zum zweiten Gefäß transportiert werden, von 0,7 bis 1,5 beträgt.
  7. Verfahren nach Anspruch 6, worin das Verhältnis von 0,8 bis 1 beträgt.
  8. Verfahren nach Anspruch 6, worin das Volumen an Wasser, welches aus dem zweiten Gefäß extrahiert wird, dem Volumen an Schlacketeilchen, welche mittels Schwerkraft zum zweiten Gefäß transportiert werden, entspricht.
  9. Verfahren nach einem der Ansprüche 1 bis 8, worin frisches Wasser in das zweite Gefäß während des Schritts (d) und/oder (e) derart zugeführt wird, daß das zweite Gefäß frisches Wasser enthält, bevor der Schritt (b) durchgeführt wird.
  10. Verfahren nach einem der Ansprüche 1 bis 9, worin das an Schlacke arme Wasser aus dem ersten Gefäß abgeführt wird.
EP00969277A 1999-09-21 2000-09-20 Verfahren zur entfernung von festschlacken aus einem wässrigen gemisch Expired - Lifetime EP1224246B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP00969277A EP1224246B1 (de) 1999-09-21 2000-09-20 Verfahren zur entfernung von festschlacken aus einem wässrigen gemisch

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
EP99307444 1999-09-21
EP99307444 1999-09-21
EP00969277A EP1224246B1 (de) 1999-09-21 2000-09-20 Verfahren zur entfernung von festschlacken aus einem wässrigen gemisch
PCT/EP2000/009254 WO2001021736A1 (en) 1999-09-21 2000-09-20 Process to remove solid slag particles from a mixture of solid slag particles and water

Publications (2)

Publication Number Publication Date
EP1224246A1 EP1224246A1 (de) 2002-07-24
EP1224246B1 true EP1224246B1 (de) 2006-11-15

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EP (1) EP1224246B1 (de)
CN (1) CN1220756C (de)
AU (1) AU764501B2 (de)
DE (1) DE60031875T2 (de)
ES (1) ES2274808T3 (de)
WO (1) WO2001021736A1 (de)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
TWI494422B (zh) * 2008-07-15 2015-08-01 Thyssenkrupp Uhde Gmbh 煤炭氣化反應器之熔渣排出裝置
TWI495717B (zh) * 2008-05-14 2015-08-11 Exxonmobil Res & Eng Co 供烴類的短接觸時間催化性裂化反應用之改良的ｆｃｃ反應器和提升管設計

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102006055050A1 (de) 2006-11-22 2008-05-29 Eos Gmbh Electro Optical Systems Vorrichtung zum schichtweisen Herstellen eines dreidimensionalen Objekts und Verfahren zum Justieren eines Optiksystems von dieser
DE102008005704A1 (de) 2008-01-24 2009-07-30 Uhde Gmbh Verfahren und Anlage zur Entfernung insbesondere bei der Synthesegas-Gewinnung anfallenden Schlacken aus einem Schlackebad-Behälter
DE102008035386A1 (de) 2008-07-29 2010-02-11 Uhde Gmbh Schlackeaustrag aus Reaktor zur Synthesegasgewinnung
WO2010040763A2 (en) 2008-10-08 2010-04-15 Shell Internationale Research Maatschappij B.V. Process to prepare a gas mixture of hydrogen and carbon monoxide
AU2009331847B2 (en) 2008-12-22 2012-06-07 Air Products And Chemicals, Inc. Process to prepare methanol and/or dimethylether

Family Cites Families (5)

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Publication number Priority date Publication date Assignee Title
DE2829629C2 (de) * 1978-07-06 1982-07-29 Ruhrchemie Ag, 4200 Oberhausen Verfahren und Vorrichtung zum Ausschleusen von Rückständen aus dem Drucksystem einer Druckvergasungsanlage
BR8105270A (pt) * 1980-11-12 1982-08-31 Texaco Development Corp Processo para producao de gas de sintese substancialmente isento de particulas
US4465496A (en) * 1983-01-10 1984-08-14 Texaco Development Corporation Removal of sour water from coal gasification slag
DE3714915A1 (de) * 1987-05-05 1988-11-24 Shell Int Research Verfahren und vorrichtung fuer die herstellung von synthesegas
JPH10287886A (ja) * 1997-04-11 1998-10-27 Babcock Hitachi Kk スラグ排出方法及び該方法を用いる装置

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
TWI495717B (zh) * 2008-05-14 2015-08-11 Exxonmobil Res & Eng Co 供烴類的短接觸時間催化性裂化反應用之改良的ｆｃｃ反應器和提升管設計
TWI494422B (zh) * 2008-07-15 2015-08-01 Thyssenkrupp Uhde Gmbh 煤炭氣化反應器之熔渣排出裝置

Also Published As

Publication number Publication date
DE60031875T2 (de) 2007-04-05
WO2001021736A1 (en) 2001-03-29
AU764501B2 (en) 2003-08-21
ES2274808T3 (es) 2007-06-01
AU7905600A (en) 2001-04-24
DE60031875D1 (de) 2006-12-28
CN1376190A (zh) 2002-10-23
EP1224246A1 (de) 2002-07-24
CN1220756C (zh) 2005-09-28

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