CN1220756C - Process to remove solid slag particles from a mixture of solid slag particles and water - Google Patents
Process to remove solid slag particles from a mixture of solid slag particles and water Download PDFInfo
- Publication number
- CN1220756C CN1220756C CN 00813191 CN00813191A CN1220756C CN 1220756 C CN1220756 C CN 1220756C CN 00813191 CN00813191 CN 00813191 CN 00813191 A CN00813191 A CN 00813191A CN 1220756 C CN1220756 C CN 1220756C
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- China
- Prior art keywords
- container
- slag
- water
- vessel
- slag particles
- Prior art date
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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
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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)
Abstract
Process to remove solid slag particles from a mixture of solid slag particles 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, by a) discharging of the mixture from the quench zone to a first vessel, (b) discharging slag particles from the first vessel to a second vessel and discharging water poor in solid slag from the second vessel, which second vessel is located below and fluidly connected to said first vessel by means of an open connecting conduit provided with pumping means and is further provided with closed means to discharge slag from its lower end, (c) fluidly closing the first vessel from the second vessel, (d) opening of the means to discharge slag from the second vessel to remove slag from the second vessel to a lower pressure zone, and (e) closing the means to discharge slag from the second vessel and repeating steps (a) to (e).
Description
The present invention relates to the method for removing solid slag in the mixture of a kind of solid slag that exists and water from quench zone, described quench zone is the part with the method for the finely divided solid carbon fuel production synthetic gas of oxygen-containing gas partial combustion.
This method is open in EP-A-290087.In this method, the mixture of water and solid slag is intermittently discharged the gasification system of pressurization.The liquid slag is for example gasification or partially combusted by product.The liquid slag is discharged by the outlet that is positioned at reactor bottom, and enters water-bath or slag quench vessel by gravity by the slag disposal facilities, forms the mixture of water and solid slag particles there.With the false bottom funnel with mixture from the gasification system intermittently discharged of pressurization to the discharge section of lower pressure.In draining period, false bottom funnel and gasification system are separated by the one or more valves that are closed in the connection line between slag quench vessel and the false bottom funnel.
A problem of this drain steps is, when the valve closes between false bottom funnel and the quench vessel, the slag that is accumulated in this valve downstream just has the tendency in the narrow space bridging of described valve downstream.After false bottom funnel and gasification system are connected again, be difficult to slag and dropped in the false bottom funnel.This problem is resolved by disclosed method among the EP-A-290087, wherein keeps constant nitrogen bubble or nitrogen cover in the false bottom funnel.Be lower than pressure in the slag quench vessel by the pressure of guaranteeing described nitrogen bubble, in the process of the valve opening between false bottom funnel and slag quench vessel, form water and slag initially to dirty.This method also makes slag be discharged into rapidly the false bottom funnel from quench vessel.
Though having confirmed aforesaid method is gratifying in business practice, still there are some shortcomings in it.A shortcoming is nitrogen to be provided and to consume relevant expense with nitrogen between each draining period by the other equipment of installation.Another shortcoming is with the mixture of discharging, also to give off sulfocompound (wherein hydrogen sulfide is topmost) and other dissolved components (for example ammonia, muriate and carbon monoxide) of some amount.Hydrogen sulfide is generated by the sulfocompound that exists in the hydrocarbon feed in reactor.Part hydrogen sulfide is dissolved in the water in the slag quench vessel, therefore is discharged with slag in above-mentioned method.
The simple method that the objective of the invention is a kind of rapid separate solid slag particles of quench zone from the mixture that contains described slag particles and water, so that can not remove sulfocompound or only remove seldom sulfocompound from quench zone with slag.
This purpose reaches by following method.The method of removing solid slag particles from quench zone in the solid slag particles that exists and the mixture of water may further comprise the steps, and described quench zone is the part with the method for the finely divided solid carbon fuel fabrication synthetic gas of oxygen-containing gas partial combustion.
(a) mixture is discharged into first container from quench zone;
(b) slag particles by gravity from first vessel discharge to second container, described second container is positioned at the below of described first container and links to each other with described first fluid container by the open type linking conduit, closing device also is housed, so that lower end discharging slag from described second container, and slag-free water is by being equipped with the conduit discharging of pumping equipment and fixing inlet, so that slag-free water is pumped out from second container;
(c) will close on first container and second fluid container;
(d) open from the equipment of the second vessel discharge slag, so as with slag from second vessel discharge to the lower pressure section; And
(e) close from the equipment of the second vessel discharge slag, and repeating step (a) is to (e).
By implementing method of the present invention, solid slag particles might be discharged from the container of mixture that liquid and solid slag particles are housed, wherein the quantity of the sulfocompound that discharges with water is lower than the method for prior art.Therefore, discharge less hydrogen sulfide with slag particles.Usually the hydrogen sulfide that discharges with slag discharges with the synthetic product gas now.Because synthesis gas contains the hydrogen sulfide of some amount usually, it is no problem removing this newly-increased hydrogen sulfide in the hydrogen sulfide stripping workshop section of existing downstream.When having read detailed description of the present invention, other advantage of the present invention will be conspicuous.
Present method relates to from the method with the finely divided solid carbon fuel production synthetic gas of oxygen-containing gas partial combustion and separates slag particles.Carbon containing incendiary example is coal, mud coal, timber, coke (for example refinery coke), cigarette ash, carbonaceous wastes, biomass (biomass) and composition thereof.The mixture of above-mentioned raw materials and metallic refuse also can be used as charging.
The volume of the slag-free water that from second container, takes out and meanwhile the ratio of the solid volume by conduit from first container to second container be preferably 0.7-1.5, more preferably 0.8-1. most preferably, take out and send into from second container liquid volume of first container with because gravity is roughly the same to the solid volume of second container from first container.Make the liquid in the connection line between first container and second container approaching mobile then.This state further makes second container sulfocompound that take out and that enter second container reduce.
Preferably, the mass rate in the linking conduit of slag particles between first container and second container is 100-150 kilogram slag particles/square metre conduit or valve sectional area/second (kilogram/rice
2/ second).
Because first container is between quench zone and second container or false bottom funnel, so there is the concentration gradient of sulfocompound, wherein the concentration of sulfocompound is lower than quench zone in first container.When the height/diameter of first container than greater than 3 the time, this concentration gradient is easy to reach.Preferably, will deliver to the lower end of first container from the slag-free water that second container takes out, so that further improve this concentration gradient.This concentration gradient is favourable, because the chance that it further makes any sulfocompound enter second container reduces.
First volume of a container is preferably identical with second container or bigger.The volume that increases is as the buffer capacity of dealing with problems, and the chance that also makes any sulfocompound enter second container in addition reduces.When in step (c) during with first container and second container closure; preferably in linking conduit, do not have slag particles or seldom slag particles is arranged; thereby reduced the chance that slag particles blocks the valve in the described conduit; thereby reduced the chance of damaging valve, and kept can be used for expecting the buffer capacity of issuable problem.Second container preferably is not too little, because too little meeting produces too high discharging frequency, the throughput of this method is reduced.Suitable is that first volume of a container is 2-3 a times of second container volume.Second volume of a container is by removing the required ability decision of slag particles.Those skilled in the art can be easy to decide optimal volume according to the size of carrying out the container that required time of step (a)-(e) and hope reduces.
By take out the water of cleaning relatively from second container, reach such attraction degree, it mainly is drawn onto second container to solid from first container.Second container must sink in step (b) process fully even as big as making solid, so that do not contained the solid zone and be rich in the solid lower region.
For further minimizing can be from first vessel discharge to second container the amount of sulfocompound, in step (d) and/or step (e), from second container, remove after the slag particles and carrying out preferably filling second container before the step (a) with cleaning water or fresh water.When slag particles enters second container, a part of cleaning water (suitable for entering the particulate volume) is discharged into first container; Or be discharged into another outlet (but not preferred).When this cleaning water entered first container, in this first container, the concentration of sulfocompound further descends, and was as discussed above.
In the present invention's one embodiment preferred, first container also is equipped with the equipment of the slag-free water of discharging.Because slag particles can enter first container from quench zone then easilier, so this is favourable, as disclosed among the GB-A-2086931.Described water can be preferably by heat-obtaining from the logistics of water coolant, cooling air or the contact of other media as the medium of cooling quench zone.Precipitation that forms on the water layer surface of using described water to destroy and/or clean to exist in quench zone and the precipitation that originally exists on one's body at quench zone equipment may also be favourable.Emit some such logistics to prevent that impurities accumulation from may be favourable.The optimum position that slag-free water discharges from first container is identical with the discussion of second container.
It is very favourable that present method is used in such a case, wherein the pressure in first container be higher than isolated solid from second vessel discharge to environmental stress.In evaporating method, in the method for the invention, quench zone is generally the 20-60 crust with pressure in relevant first container, and solid is approximately discharging from second container (being sometimes referred to as the false bottom funnel container) under the environmental stress usually.
Accompanying drawing represents to implement the equipment of the preferred embodiment of above-mentioned the inventive method.Described equipment comprises first container (1), second container (2), first conduit (3) and second conduit (4) that are preferably placed at first container below and link to each other with second fluid container with first container.First conduit (3) is preferably placed at such position, so that the slag particles in step (b) can move to second container (2) from first container (1) by gravity.Second conduit (4) is equipped with pumping equipment (5), so as the water that will not contain slag particles from second container transport to first container.The equipment that is applicable to pumping liquid for example is toothed gear pump, lobe pump, rotor pump, impeller pump or riser tube.The inlet of second conduit (4) is positioned at such position, and the water that does not consequently contain slag particles is pumped into first container (1) from second container (2).The slag particles that enters second container (2) by conduit (3) will be in the accumulation of the bottom of second container, and consequently the top of second container does not contain slag particles with respect to the bottom.
Therefore preferably, the inlet (6) of conduit (4) is positioned at the top of second container (2), and away from the exit opening (8) of first conduit (3) that enters second container (2).More preferably, the outlet (8) that tubular-baffle (7) is placed on conduit (3) on every side, it moves downward the slag particles that enters second container, and away from the inlet (6) of second conduit (4).And second container is equipped with exit opening (9), and solid particulate can discharge by it, and first container is equipped with the inlet opening (10) that is used for receiving from the mixture of quench zone (14).Opening (10) can be chosen wantonly pulverizer is housed, so that entering before first container big slag particles fragmentation.If there is not the slag pulverizer, opening (10) is bigger than the opening in the conduit that connects first container (1) and second container (2) usually so, thereby can make the slag particles stream that does not have turbulent flow enter first container from quench zone (14).
Accompanying drawing also is illustrated in the valve (11,13) in conduit (3) and (9), so that operate present method in discharge mode of the present invention.In step (c), valve (11) is closed and pump (5) stops.In step (d), valve (13) is shown in an open position, so that slag particles is discharged from second container (2).Accompanying drawing also illustrates discharge section (12).
Accompanying drawing also illustrates the conduit (15) that slag-free water can be removed by it from first container, and with the identical tubular-baffle (16) on function of the baffle plate (7) described in second container.
To the present invention be described with following non-limiting example.
In experimental installation as shown in Figure 2, container 1 is equipped with water and 2335 kilograms/meter of the density that made by coal gasification process
3The mixture of 172 kilograms of slags.Most of slag particles is near container 1 bottom valve 11.Container 2 is equipped with cleaning water.Diameter is after 10 centimetres valve 11 is opened and pump 5 starts, to observe the stable discharging current by valve.The flow velocity of pump is 15.5 liters/minute, and has 172 kilograms of slags to discharge in 3.65 minutes.Liquid by conduit (4) from second container transport to first container is with the solid volume ratio by conduit (3) is 0.75 therefore among this embodiment in contemporaneously mutually.
Embodiment 2
Repeat embodiment 1, the flow velocity of different is pump is 36.3 liters/minute.In 2.44 minutes, discharge 172 kilograms of identical slags.Liquid by conduit (4) from second container transport to first container is with the solid volume ratio by conduit (3) is 1.18 among this embodiment in contemporaneously mutually.
The comparative example A
Repeat embodiment 1, different is not use pump 5.Flow by valve 5 is very unstable, and therefore experiment repeats 15 times, so that obtain reliable test-results.Average 172 kilograms of slags passed through valve 11 in 5.6 minutes.
Above-mentioned experimental result shows, uses method of the present invention, and the slag of high flow rate can be from top container transport to following container, reduces above described container transport simultaneously to the described water yield of surface vessel down.
Claims (9)
1. the method for removing solid slag particles in the mixture of solid slag particles from quench zone (14) and water, described quench zone (14) is that described method comprises with the part of the method for the finely divided solid carbon fuel fabrication synthetic gas of oxygen-containing gas partial combustion:
(a) described mixture is discharged into first container (1) from quench zone (14),
(b) slag particles by gravity from first container, (1) is discharged into second container, (2), described second container, (2) be positioned at described first container, (1) the open type linking conduit is also passed through in below, (3) with described first container, (1) fluid links to each other, switching device also is housed, (13), so that lower end discharging slag from described second container, and slag-free water is by being equipped with pumping equipment, (5) and fixing inlet, (6) conduit, (4) discharging, so that slag-free water is from second container, (2) be pumped out
(c) will close on first container (1) and second container (2) fluid,
(d) open the equipment (13) of slag from second container (2) discharging, so that slag is discharged into the lower pressure section from second container (2), and,
(e) close the equipment (13) of slag from second container (2) discharging, and repeating step (a) is to (e), wherein in the process fresh water is sent into second container (2), make that second container (2) just contains fresh water before implementation step (b) in step (d) and/or (e).
2. according to the process of claim 1 wherein the slag-free water that obtains is delivered to first container (1) in step (b).
3. according to the method for claim 2, wherein slag-free water is delivered to the lower end of first container (1), the height of described first container (1)/diameter ratio is greater than 3.
4. according to each method among the claim 1-3, wherein do not contain the top discharging of solid water from second container (2), its position is away from the exit opening (8) of first conduit (3) that enters second container (2).
5. according to the method for claim 4, wherein tubular-baffle (3) at the exit opening (8) of first conduit (3) on every side, the slag particles that enters second container (2) is moved downward and away from conduit (4) inlet (6), the water that does not contain slag particles pumps out from described second container (2) by this duct entry.
6. according to each method among the claim 1-3, wherein the water that takes out from second container (2) is 0.7-1.5 with the volume ratio that is transported to the solid slag particles of second container (2) in contemporaneously mutually.
7. according to the method for claim 6, wherein said ratio is 0.8-1.
8. according to the method for claim 6, wherein the volume of the water that takes out from second container (2) equals to be transported to the volume of the slag particles of second container (2).
9. according to each method among the claim 1-3, wherein slag-free water discharges from first container (1).
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP99307444.2 | 1999-09-21 | ||
EP99307444 | 1999-09-21 |
Publications (2)
Publication Number | Publication Date |
---|---|
CN1376190A CN1376190A (en) | 2002-10-23 |
CN1220756C true CN1220756C (en) | 2005-09-28 |
Family
ID=8241629
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
CN 00813191 Expired - Lifetime CN1220756C (en) | 1999-09-21 | 2000-09-20 | Process to remove solid slag particles from a mixture of solid slag particles and water |
Country Status (6)
Country | Link |
---|---|
EP (1) | EP1224246B1 (en) |
CN (1) | CN1220756C (en) |
AU (1) | AU764501B2 (en) |
DE (1) | DE60031875T2 (en) |
ES (1) | ES2274808T3 (en) |
WO (1) | WO2001021736A1 (en) |
Families Citing this family (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE102008005704A1 (en) | 2008-01-24 | 2009-07-30 | Uhde Gmbh | Process and installation for the removal of slag from a slag bath tank, in particular in synthesis gas recovery |
US8349170B2 (en) * | 2008-05-14 | 2013-01-08 | Exxonmobil Research And Engineering Company | FCC reactor and riser design for short contact-time catalytic cracking of hydrocarbons |
DE102008033095A1 (en) * | 2008-07-15 | 2010-01-28 | Uhde Gmbh | Apparatus for slag removal from a coal gasification reactor |
DE102008035386A1 (en) | 2008-07-29 | 2010-02-11 | Uhde Gmbh | Slag discharge from reactor for syngas recovery |
EP2334765A2 (en) | 2008-10-08 | 2011-06-22 | Shell Internationale Research Maatschappij B.V. | Process to prepare a gas mixture of hydrogen and carbon monoxide |
EP2373602B1 (en) | 2008-12-22 | 2013-08-21 | Shell Internationale Research Maatschappij B.V. | Process to prepare methanol and/or dimethylether |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2829629C2 (en) * | 1978-07-06 | 1982-07-29 | Ruhrchemie Ag, 4200 Oberhausen | Method and device for discharging residues from the pressure system of a pressure gasification plant |
BR8105270A (en) * | 1980-11-12 | 1982-08-31 | Texaco Development Corp | PROCESS FOR THE PRODUCTION OF SYNTHESIS GAS SUBSTANTIALLY FREE OF PARTICLES |
US4465496A (en) * | 1983-01-10 | 1984-08-14 | Texaco Development Corporation | Removal of sour water from coal gasification slag |
DE3714915A1 (en) * | 1987-05-05 | 1988-11-24 | Shell Int Research | METHOD AND DEVICE FOR THE PRODUCTION OF SYNTHESIS GAS |
JPH10287886A (en) * | 1997-04-11 | 1998-10-27 | Babcock Hitachi Kk | Discharging method of slag and apparatus by using the same |
-
2000
- 2000-09-20 AU AU79056/00A patent/AU764501B2/en not_active Expired
- 2000-09-20 DE DE60031875T patent/DE60031875T2/en not_active Expired - Lifetime
- 2000-09-20 CN CN 00813191 patent/CN1220756C/en not_active Expired - Lifetime
- 2000-09-20 EP EP00969277A patent/EP1224246B1/en not_active Expired - Lifetime
- 2000-09-20 ES ES00969277T patent/ES2274808T3/en not_active Expired - Lifetime
- 2000-09-20 WO PCT/EP2000/009254 patent/WO2001021736A1/en active Search and Examination
Also Published As
Publication number | Publication date |
---|---|
AU764501B2 (en) | 2003-08-21 |
AU7905600A (en) | 2001-04-24 |
WO2001021736A1 (en) | 2001-03-29 |
ES2274808T3 (en) | 2007-06-01 |
EP1224246B1 (en) | 2006-11-15 |
DE60031875D1 (en) | 2006-12-28 |
CN1376190A (en) | 2002-10-23 |
DE60031875T2 (en) | 2007-04-05 |
EP1224246A1 (en) | 2002-07-24 |
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Effective date of registration: 20180813 Address after: American Pennsylvania Patentee after: Air Products and Chemicals, Inc. Address before: Holland Hague Patentee before: Shell Internationale Research Maatschappij B. V. |
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