AU764501B2 - 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
- AU764501B2 AU764501B2 AU79056/00A AU7905600A AU764501B2 AU 764501 B2 AU764501 B2 AU 764501B2 AU 79056/00 A AU79056/00 A AU 79056/00A AU 7905600 A AU7905600 A AU 7905600A AU 764501 B2 AU764501 B2 AU 764501B2
- Authority
- AU
- Australia
- Prior art keywords
- vessel
- slag
- water
- slag particles
- process according
- 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
Links
- 239000002893 slag Substances 0.000 title claims description 85
- 239000002245 particle Substances 0.000 title claims description 45
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims description 40
- 238000000034 method Methods 0.000 title claims description 38
- 230000008569 process Effects 0.000 title claims description 36
- 239000007787 solid Substances 0.000 title claims description 36
- 239000000203 mixture Substances 0.000 title claims description 18
- 238000010791 quenching Methods 0.000 claims description 27
- 239000007789 gas Substances 0.000 claims description 8
- 230000015572 biosynthetic process Effects 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 6
- 230000005484 gravity Effects 0.000 claims description 6
- 238000003786 synthesis reaction Methods 0.000 claims description 6
- 238000002485 combustion reaction Methods 0.000 claims description 5
- 239000000446 fuel Substances 0.000 claims description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 238000002360 preparation method Methods 0.000 claims description 4
- 239000013505 freshwater Substances 0.000 claims description 3
- 238000005086 pumping Methods 0.000 claims description 3
- 230000000052 comparative effect Effects 0.000 claims description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical class [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 10
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 8
- 239000007788 liquid Substances 0.000 description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 7
- 238000002309 gasification Methods 0.000 description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- 229910052799 carbon Inorganic materials 0.000 description 5
- 229960005419 nitrogen Drugs 0.000 description 5
- 239000003245 coal Substances 0.000 description 3
- 150000001875 compounds Chemical class 0.000 description 3
- 229910001873 dinitrogen Inorganic materials 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 241001248539 Eurema lisa Species 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000003415 peat Substances 0.000 description 1
- 239000002006 petroleum coke Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
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
- C10J3/46—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
Landscapes
- 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)
Description
WO 01/21736 1 PCT/EPOO/09254 PROCESS TO REMOVE SOLID SLAG PARTICLES FROM A MIXTURE OF SOLID SLAG PARTICLES AND WATER 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.
Such a process is described in EP-A-290087. In this process a mixture of water and solid slag is batchwise sluiced out of a pressurised gasification system. Liquid slag is a by-product of the gasification or partial combustion of, for example, coal. Liquid slag is drained through the outlet located at the reactor bottom and passed by gravity through a slag discharge means into a water bath or slag quenching vessel where the mixture of water and solid slag particles are formed. The batchwise sluicing of the mixture from the pressurized gasification system to a lower-pressure discharge zone is performed by means of a lockhopper. During the sluicing cycle the lockhopper is isolated from the gasification system by closing one or more valves in the connecting line between the slag quench vessel and the lockhopper.
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. By ensuring that the pressure of the said nitrogen gas bubble is lower than the pressure in the slag quench vessel an initial downwards flow of water and slag during opening of the valves between the lockhopper and the slag quench vessel is achieved. This method also results in a quick discharge of the slag from the quench vessel into the lockhopper.
Although the above process has proven to work satisfactorily in commercial practice it still has some disadvantages. 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 to provide 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 or to provide a useful alternative to the prior 20 art.
2 Accordingly, there is provided a process to remove solid slag particles from a mixture of solid slag particles and water present in the quench zone, which quench zone is •part of a process for the preparation of synthesis gas by partial combustion of *o [R:\LIBZZ]588894spccidoc:gym 14-09-2001 EPO D EP000925, EPO -DG 3- 1 09. 2001 finely dispersed solid carbon-containing fuel with oxygen-containing gas, by discharging of the mixture from the quench zone to a first vessel, discharging slag particles from the first vessel to a second vessel by means of gravity, which second vessel is located below and fluidly connected to said first vessel by means of an open connecting conduit and is further provided with closed means to discharge slag from its lower end, and discharging water poor in solid slag from the second vessel via a conduit provided with pumping means and having an inlet locatedsuch that water poor in slag particles are pumped from the second vessel, fluidly closing the first vessel from the second vessel, opening of the means to discharge slag from the second vessel to remove slag from the second vessel to a lower pressure zone, and closing- the means to di.scharge slag-from the second vessel and repeating steps to By performing the process according the invention it is possible to discharge solid slag particles from a vessel containing a mixture of liquid and solid slag particles, wherein the amount of sulphur containing compounds being discharged together with the water is lower than in prior art processes. Less hydrogen sulphide will thus be discharged together with the slag particles.
The hydrogen sulphide normally discharged together with the slag will now be discharged with the synthesis product gasses. Because the synthesis gasses typically contain a certain amount of hydrogen sulphide it will be no problem to remove this additional amount of hydrogen sulphide in the existing downstream hydrogen sulphide AMENDED SHEET 14-09-2001 EP000925i 3a removal sections. Further advantages of the present process will become apparent when reading the detailed description of this invention.
N:\M\TS0919PCT AMENDED SHEET WO 01/21736 PCT/EP00/09254 4 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.
Examples of 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 i. Most preferably 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.
Preferably 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) Because a first vessel is present between the quench zone and the second vessel or lockhopper 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 WO 01/21736 PCT/EP00/09254 5 than three. Preferably 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 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. Suitably 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 and the desire to minimise the size of the vessels.
By extracting relatively clean water from the second vessel a sort of suction is achieved which predominately pulls the solids from the first vessel to the second vessel. The second vessel must be large enough to enable the solids to settle sufficiently during step in order to achieve a region which is poor in solids and a lower region which is rich in solids.
14-09-2001 EP000925L 6 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 before performing step When 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.
When 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.
In a preferred embodiment of the present invention the first vessel is also provided with means to discharge water poor in slag. This is advantageous because slag particles can then more easily enter the first vessel from the quench zone as is described in GB-A-2086931.
This water can advantageously be used-as medium to cool the quench zone by extracting heat from 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 AMENDED SHEET 14-09-2001 EP000925 6a vessel. In a gasification process the pressure in the quench zone and the associated first vessel in the N:\M\TS0919PCT AMENDED SHEET WO 01121736 PCT/EP00/09254 -7process according the invention, is typically between 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 a second vessel preferably positioned below the first vessel, and a first and second conduit fluidly connecting the first and second vessel. The first conduit is preferably located such that slag particles in step (b) can move by gravity from the first vessel to the second vessel Second conduit is provided with pumping means 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 is located such that water which is poor in slag particles is pumped from the second vessel into the first vessel Slag particles entering second vessel via conduit 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.
Preferably the inlet of conduit is therefore located in the upper part of the second vessel and away from the outlet opening of the first conduit (3) entering the second vessel More preferably a tubular shield is present around the outlet of conduit which directs the slag particles entering the second vessel downwards and away from the inlet of the second conduit The second vessel is furthermore provided with an outlet opening through which solid particles can be discharged and the first vessel is WO 01/21736 PCT/EP00/09254 8 provided with an inlet opening (10) for receiving the mixture from the quench zone 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 and second vessel, thereby enabling a trouble free flow of slag particles into the first vessel from the quench zone (14).
The Figure also shows valves (11, 13) present in conduits and in order to operate the process in a sluice mode according to the present invention. In step valve (11) is closed and pump is stopped. In step valve (13) is in a open position to discharge the slag particles from the second vessel 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 described in the second vessel.
The invention shall be illustrated by the following non-limiting Examples.
Example 1 In an experimental set-up as illustrated in Figure 2 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 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 WO 01/21736 PCT/EP00/09254 9 volume of liquid which is transported from the second vessel to the first vessel via conduit relative to the volume of solids passing conduit in the same time period is in this example thus 0.75.
Example 2 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 relative to the volume of solids passing conduit in the same time period is in this example 1.18.
Comparative experiment A 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.
The above experimental results show that by using the process according to the invention a high flow of slag can be transported from an upper vessel to a lower vessel while minimizing the amount of water being transported from said upper vessel to said lower vessel.
Claims (11)
1. A 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 discharging of the mixture from the quench zone to a first vessel, discharging slag particles from the first vessel to a second vessel by means of gravity, which second vessel is located below and fluidly connected to said first vessel by means of an open connecting conduit and is further provided with closed means to discharge slag from its lower end, and discharging water poor in solid slag from the second vessel via a conduit provided with pumping means and having an inlet located such that water poor in slag particles are pumped from the second vessel, fluidly closing the first vessel from the second vessel, opening of the means to discharge slag from the second vessel to remove slag from the second vessel to a lower pressure zone, and closing the means to discharge slag from the second vessel and repeating steps to
2. The process according to claim 1, wherein the water poor in slag obtained in step is supplied to the first vessel. 20
3. The process according to claim 2, wherein the water poor in slag is supplied to the lower end of a first vessel, which first vessel has a height over diameter ratio of more than three.
4. The process according to any one of claims 1-3, wherein the water, which is .oo D poor in solids, is discharged from the upper part of the second vessel at a position away from the outlet opening of the first conduit entering the second vessel.
The process according to claim 4, wherein a tubular shield is present around the outlet opening of the first conduit directing the slag particles entering the second vessel downwards and away from the inlet of the conduit through which water poor in slag particles is pumped from said second vessel.
6. The process according to any one of claims 1-5, wherein the ratio of volume of water, which is extracted from the second vessel, relative to the volume of solid slag o. particles being transported to the second vessel in the same time period is between 0.7 S.. and
7. The process according to claim 6, wherein the ratio is between 0.8 and 1. [R:\LJBZZ]5SSS94speci.doc:gym 11
8. The process according to claim 6, wherein the volume of water extracted from the second vessel is equal to the volume of slag particles being transported to the second vessel due to gravity.
9. The process according to any one of claims 1-8, wherein fresh water is supplied to the second vessel during step and/or resulting in that second vessel contains fresh water before step is performed.
The process according to any one of claims 1-9, wherein water poor in slag is discharged from the first vessel.
11. A process to remove solid slag particles from a mixture of solid slag particles and water present in a quench zone substantially as hereinbefore described with reference to any one of the examples but excluding the comparative examples. Dated 24 June, 2003 Shell Internationale Research Maatschappij B.V. Patent Attorneys for the Applicant/Nominated Person SPRUSON FERGUSON S. S S S S oo oo t [R:\LIBZZ]58894spcci.doc:gym
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP99307444 | 1999-09-21 | ||
| EP99307444 | 1999-09-21 | ||
| 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 |
|---|---|
| AU7905600A AU7905600A (en) | 2001-04-24 |
| AU764501B2 true AU764501B2 (en) | 2003-08-21 |
Family
ID=8241629
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU79056/00A Expired AU764501B2 (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 (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102006055050A1 (en) | 2006-11-22 | 2008-05-29 | Eos Gmbh Electro Optical Systems | Apparatus for layering a three-dimensional object and method for adjusting an optical system therefrom |
| 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 |
| 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 |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2086931A (en) * | 1980-11-12 | 1982-05-19 | Texaco Development Corp | Ash removal and synthesis gas generation from coal |
Family Cites Families (4)
| 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 |
| 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 WO PCT/EP2000/009254 patent/WO2001021736A1/en not_active Ceased
- 2000-09-20 DE DE60031875T patent/DE60031875T2/en not_active Expired - Lifetime
- 2000-09-20 EP EP00969277A patent/EP1224246B1/en not_active Expired - Lifetime
- 2000-09-20 AU AU79056/00A patent/AU764501B2/en not_active Expired
- 2000-09-20 ES ES00969277T patent/ES2274808T3/en not_active Expired - Lifetime
- 2000-09-20 CN CN 00813191 patent/CN1220756C/en not_active Expired - Lifetime
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2086931A (en) * | 1980-11-12 | 1982-05-19 | Texaco Development Corp | Ash removal and synthesis gas generation from coal |
Also Published As
| Publication number | Publication date |
|---|---|
| DE60031875T2 (en) | 2007-04-05 |
| WO2001021736A1 (en) | 2001-03-29 |
| EP1224246B1 (en) | 2006-11-15 |
| ES2274808T3 (en) | 2007-06-01 |
| AU7905600A (en) | 2001-04-24 |
| DE60031875D1 (en) | 2006-12-28 |
| CN1376190A (en) | 2002-10-23 |
| EP1224246A1 (en) | 2002-07-24 |
| CN1220756C (en) | 2005-09-28 |
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