GB2259521A - Moving bed coal gasifier - Google Patents
Moving bed coal gasifier Download PDFInfo
- Publication number
- GB2259521A GB2259521A GB9218050A GB9218050A GB2259521A GB 2259521 A GB2259521 A GB 2259521A GB 9218050 A GB9218050 A GB 9218050A GB 9218050 A GB9218050 A GB 9218050A GB 2259521 A GB2259521 A GB 2259521A
- Authority
- GB
- United Kingdom
- Prior art keywords
- coal
- gasifier
- moving bed
- split
- particulates
- 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.)
- Withdrawn
Links
- 239000003245 coal Substances 0.000 title claims abstract description 103
- 239000007789 gas Substances 0.000 claims abstract description 40
- 239000002737 fuel gas Substances 0.000 claims abstract description 38
- 238000002485 combustion reaction Methods 0.000 claims abstract description 26
- 239000011269 tar Substances 0.000 claims abstract description 26
- 238000006243 chemical reaction Methods 0.000 claims abstract description 23
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 15
- 239000007800 oxidant agent Substances 0.000 claims abstract description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 10
- 230000001590 oxidative effect Effects 0.000 claims abstract description 10
- 239000000567 combustion gas Substances 0.000 claims abstract description 8
- 229930195733 hydrocarbon Natural products 0.000 claims description 10
- 150000002430 hydrocarbons Chemical class 0.000 claims description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 5
- 229910052760 oxygen Inorganic materials 0.000 claims description 5
- 239000001301 oxygen Substances 0.000 claims description 5
- 239000002002 slurry Substances 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000011236 particulate material Substances 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 2
- 239000004215 Carbon black (E152) Substances 0.000 claims 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 abstract description 23
- 238000002309 gasification Methods 0.000 abstract description 17
- 229910021529 ammonia Inorganic materials 0.000 abstract description 11
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 9
- 229910052717 sulfur Inorganic materials 0.000 description 9
- 239000011593 sulfur Substances 0.000 description 9
- 238000000034 method Methods 0.000 description 7
- 239000002594 sorbent Substances 0.000 description 5
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000000197 pyrolysis Methods 0.000 description 2
- 229910001308 Zinc ferrite Inorganic materials 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000004513 sizing Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000011282 treatment Methods 0.000 description 1
- 239000011800 void material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- WGEATSXPYVGFCC-UHFFFAOYSA-N zinc ferrite Chemical compound O=[Zn].O=[Fe]O[Fe]=O WGEATSXPYVGFCC-UHFFFAOYSA-N 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
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/20—Apparatus; Plants
-
- 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
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/20—Apparatus; Plants
- C10J3/22—Arrangements or dispositions of valves or flues
- C10J3/24—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed
- C10J3/26—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed downwardly
-
- 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
- C10J3/723—Controlling or regulating the gasification process
-
- 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
- C10J2200/00—Details of gasification apparatus
- C10J2200/36—Moving parts inside the gasification reactor not otherwise provided for
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Industrial Gases (AREA)
Abstract
A moving bed coal gasifier 10 for the production of tar-free, low ammonia fuel gas, employs a combustion zone 20 in a free-board area above the moving bed 24 to burn coal fines to provided hot combustion gases for pyrolyzing and gasifying coal particulates in the moving bed to form fuel gas as the hot gases move co-currently with the downwardly moving coal particulates. The fuel gas contains entrained tars and ammonia compounds which contact hot char and ash in the moving bed and are cracked so that the fuel gas removed from the gasifier at a mid-point off-take 40 is essentially tar-free and of low ammonia content. Concurrently with this gasification reaction, steam and an oxidant are introduced into a region below the moving bed to flow countercurrently to the downwardly moving bed to contact and react with carbon remaining in the char to create additional fuel gas which is, also extracted from the gasifier at the mid-point off-take 40. <IMAGE>
Description
SPLIT FLOW GASIFIER
BACKGROUND OF THE INVENTION
The present invention relates generally to a moving bed gasifier for the production of fuel gas, and more particularly to a moving bed gasifier having a gas take-off intermediate upper and lower ends of the gasifier and which provides essentially tar-free and low-ammonia fuel gas. The United States Government has rights in this invention pursuant to the employer-employee relationship of the U. S. Department of Energy and the inventor.
Coal gasification techniques used for the production of fuel gas have been practiced in various gasifier configurations and systems including those utilizing fixed, moving and fluidized bed concepts. Of these various gasification systems, the gasifiers employing moving beds have received wide acclaim and usage. In a typical operation of a moving bed gasifier, particulate coal is introduced into the reaction vessel of the gasifier through the upper end thereof while an oxidant and high temperature steam are introduced into the reactor vessel through the lower end thereof for passage upwardly or countercurrently to the downwardly moving bed of coal. As the oxidant and steam contact the moving particulates in a lower portion of the moving bed of coal, the coal particulates are sufficiently heated to provide a reaction capable of producing gaseous products including fuel gas.These gaseous products passing countercurrently to the moving bed of coal, heat the coal sufficiently to volatize the coal to effect the release of hydrocarbons and tars from the coal in the upper portion of the moving bed. These volatilization products including tars are discharged along with the fuel gas through the top end of the gasifier.
The removal of the vol atizati on products and tars from the fuel gas have presented considerable difficulties and problems.
For example, various water scrubbers, condensers, and the like are often used to separate the tars and other condensibles from the fuel gas. Such removal techniques, in turn, present other cleanup problems such as the cleaning of the waste water from the scrubbers. Also, sulfur species contained in vol atizati on products are responsible for environmental pollution problems but the removal of such sulfur species from gas streams containing tars have been found to present some problems. For example, the presence of tars in the gases being treated effectively limits the use of particulate sulfur sorbents such as zinc ferrite since sulfur in the tars is not removed by such sorbents. Also, the tars can destructively coat and plug the sorbent.Thus, in order to use such particulate sorbents the tars must first be removed from the gas stream by employing condensation or other procedures.
The tar-removing treatments of the gas stream significantly reduce the temperature of the gas stream and presents a clean-up problem for the condensed tars. The required cooling of the gas stream for the removal of tars prevents the extraction of heat values in the gases in a heat engine such as a turbine or the like.
A still further problem encountered with the use of presently known moving bed gasifiers is that coal fines, i.e., coal particulates of a size less than about 0.25 inch, in the coal feed introduced in the gasifier through the top end thereof are essentially instantly entrained by the upwardly flowing gases and are carried out of the gasifier along with these gases so as to introduce a further clean-up problem while decreasing the overall efficiency of the gasification system with respect to the coal utilization. To overcome this problem, the size distribution of the coal particulates fed to the gasifier is maintained in a relatively narrow range so as to minimize the introduction of coal fines into the gasifier.
SUMMARY OF THE INVENTION
Accordingly, it is a principle aim or objective of the present invention to obviate or substantially minimize the above and other problems and shortcomings encountered during the use of moving bed gasifiers for the production of fuel gas. The present invention is directed to a moving bed gasifier arrangement which is capable of producing a discharge stream of high temperature fuel gas which is essentially tar-free and contains relatively low concentrations of ammonia species. In accordance with the present invention, the moving bed gasifier is constructed in such a manner that the tars and hydrocarbons devolatilized from the coal are passed downwardly through a bed of hot coal char before exiting the gas off-take positioned on the gasifier at a location substantially midway or intermediate the upper and lower ends thereof.This contacting of the tars and hydrocarbons with the hot char causes the tars and ammonia to crack and thereby effectively remove the tars and ammonia from the fuel gas stream.
Generally, the gasifier of the present invention is a splitflow gasifier comprising an elongated vertically oriented reactor means having upper, lower, and intermediate regions. Means are provided for introducing coal particulates including coal fines into the upper region of the gasifier to form a bed of coal particulates moving downwardly through the intermediate region of the gasifier. Means are also provided for introducing a stream of combustion supporting medium or oxidant into the upper region for effecting therein the combustion of the coal fines to provide a stream of hot combustion gases. This hot gas stream is contactable with downwardly moving coal particulates within an upper portion of the moving bed for reacting with these coal particulates to provide a stream of gaseous products including fuel gas while producing char and ash.Means are employed for introducing a gaseous oxidant and steam into the lower region of the gasifier for contacting and reacting with carbon values in the char entering into a lower portion of moving bed to provide a further stream of gaseous products including fuel gas. Discharge means or gas off-take means are in registry with the intermediate region and the moving bed at a location thereon substantially between the aforementioned upper and lower portions thereof for removing the gaseous products from the gasifier.
The moving-bed coal gasifier of the present invention as generally described above, can utilize a coal-water slurry or the injection of steam at the upper end thereof with a dry coal feed so as to enhance the fuel gas producing reactions by enabling a steam-carbon reaction to occur with the coal during the pyrolysis and gasification thereof. The gasifier is provided with baffle means near the mid-point gas off-take means to permit the withdrawal of the essentially particulate-free fuel gases through the gas off-take means. The baffle means also provides for the continuous flow of coal char, ash and any remaining coal passed the gas off-take means for the gasification of carbon values remaining in any coal and the coal char in the lower portion of the moving bed.
By employing the gasifier of the present invention, the sizing of coal as heretofore required for forming the moving bed is no longer required since in the present gasifier the coal fines are combusted in the upper region of the gasifier to provide the hot gases necessary for the endothermic pyrolysis and gasification reactions occurring in the moving bed.
The fuel gas discharged from the gasifier is at a relatively high temperature and can be directly used in applications where the heat energy in the high temperature gas can be effectively utilized such as in a turbine-driven electrical power generation system. With the present invention, the tars as well as the ammonia species are significantly removed or reduced from the fuel gas while within the confines of the gasifier, thus minimizing any reduction of gas temperature required for gas clean-up procedures such as the removal of sulfur species from the fuel gas in a sorbent bed downstream of the gasifier.
Other and further objects of the present invention will become obvious upon an understanding of the illustrative embodiment about to be described or will be indicated in the appended claims, and various advantages not referred to herein will occur to one skilled in the art upon employment of the invention in practice.
DESCRIPTION OF THE DRAWING
The figure is a sectional schematic view illustrating the moving bed gasifier arrangement of the present invention in which oxidants are introduced at opposite ends of the gasifier vessel while the product gas is withdrawn from the mid-point of the gasifier.
DETAILED DESCRIPTION OF THE INVENTION
As generally described above, the present invention is directed to a moving bed coal gasification apparatus which represents a considerable departure from the construction and the operational features of previously known moving bed gasifiers and which provides an essentially tar-free and low ammonia stream of fuel gas. The tar-free and low ammonia characteristics of the fuel gas extracted from the moving bed of the gasifier of the present invention effectively eliminate the extensive and costly cleanup procedures as heretofore required for fuel gas generated in moving bed gasifiers before the gas could be utilized in an envisioned application.
With reference to the figure, a moving bed coal gasifier embodying features of the present invention is generally shown at 10 and comprises a reaction vessel 12 of an elongated, vertically oriented and cylindrical configuration closed at both the top end 14 and the bottom end 16. The interior of the reaction vessel 12 is divided essentially into three vertically spaced regions as generally provided by an upper region 18 which contains a combustion zone 20 for providing a stream of hot gaseous products produced by the burning of coal particulates, especially coal fines. An intermediate region 22 in registry with the upper region 18 contains a moving bed 24 of coal particulates which are to be pyrolyzed and gasified by the hot gases discharged from the combustion zone 20 as the coal particulates move downwardly through the moving bed 24.The reaction vessel 12 is also provided with a lower region 26 which is in registry or merges with the lower portion of the moving bed 24 for completing the gasification of essentially any carbon remaining in the char resulting from the pyrolization and gasification of the coal in an upper portion of the moving bed 24 as the char moves downwardly into the lower portion of the moving bed 24 so as to significantly increase the overall efficiency of the coal gasification operation.
As shown in the figure, coal particulates which include coal fines of a particle size less than about 0.25 inch from a suitable supply (not shown) are introduced through conduit 28 into the top end 14 of the gasifier into a free-board area in the upper region 18 overlying the moving bed 24 that defines the combustion zone 20. Concurrently, with the feeding of the coal particulates into the combustion zone 20, a stream of combustion supporting medium or oxidant (air or oxygen) is introduced into the combustion zone 20 through the top end 14 of the gasifier via conduit 29 to support combustion of coal fines within the combustion zone 20.
This combustion of the coal provides a stream of hot combustion products which as generally indicated by the arrows 30 are directed downwardly into the moving bed 24 for co-current flow with the coal particulates therein as generally shown by the arrows 32.
The coal particulates introduced into the gasifier through the conduit 28 are preferably evenly spread over the moving bed by employing a suitable bed stirring and leveling device such as generally shown at 34. Alternatively, multiple inlet ports for the coal feed could be utilized to provide a relatively level upper surface on the moving bed for achieving the desired definition of the combustion zone 20. The coal feed can contain coal fines in a concentration of about 5 to 50 percent of the coal feed. The non-fine coal particulates are of a size in the range of about 0.25 inch to 2 inches. This coal in the feed may be mixed with water to form a coal-water slurry prior to the introduction thereof into the gasifier 10. Alternatively, the coal can be introduced into the gasifier as a dry feed. In such an instance, steam is preferably injected into the gasifier through conduit 36.The addition of the water, in the slurry or as steam, enables a steam-carbon reaction to occur in the moving bed 24 to significantly increase the heating value and the quantity of the fuel gas generated by the reaction of the hot combustion gases with the coal particulates. If desired, a stream of coal fines can be injected directly into the combustion zone 20 through line 38. A stream of air through line 39 may be used to disperse the coal fines within the combustion zone 20.
In order to assure that the gasification reaction occurring in the moving bed is an endothermic reaction, the oxidation conditions within the combustion zone 20 are preferably maintained at near stoichiometric or sub-stoichiometric levels. It is only necessary that combustion of the coal fines in the combustion zone 20 provide a sufficient quantity of hot combustion products to effect the endothermic gasification reaction of the coal particulates and the steam-carbon reaction in the moving bed as these combustion gases pass downwardly through a portion of the moving bed.
Coal particulates in the moving bed 24 and the gaseous products of combustion from the combustion zone 20 move cocurrently downwardly through the upper portion of the intermediate region 22 towards a off-take or discharge port 40 which is located generally between the upper and lower regions 18 and 26. The hot, essentially reducing, gases produced in the combustion zone 20 contact the coal particulates in the moving bed to sequentially dry, pyrolyze, and gasify the coal to form a gaseous product, as generally shown by the arrows 41, and which is primarily formed of fuel gas containing tars, sulfur species, ammonia compounds, and other hydrocarbons. As this endothermic gasification reaction occurs, the gas and solid temperatures are continually reduced until the gases 41 reach the level of the off-take line 40.
During these reactions, the tars and volatile hydrocarbons released from the coal in the uppermost part or portion of the intermediate region 22 are entrained by the combustion gases and by the fuel gas being generated in the moving bed so as to force them downwardly through the moving bed where these tars and hydrocarbons contact hot char and ash being generated by the reactions as generally shown by the arrows 42 so as to cause the tars and hydrocarbons to crack before the gases reach the off-take line 40. This cracking essentially removes the tars and ammonia compounds from the fuel gas being discharged from the gasifier 12.
In order to assure that the gases produced within the gasifier can be withdrawn from the gasifier through the off-take 40 essentially free from particulate material, the interior of the gasifier vessel 12 at the point of gas off-take is preferably provided with baffle means 44 for creating an essentially particle-free annular volume 46 near the inner walls of the gasifier. These baffle means permit partially gasified char and the ash particulates to proceed downwardly through the gas offtake portion of the moving bed while the tar-free, low ammonia fuel gas is separated from the particulate materials and withdrawn from the gasifier through the conduit 40.These baffle means 44 may be suitably provided by employing an annular, downwardly and inwardly inclined upper wall 48 which extends into the vessel interior a sufficient distance to permit passage of the char and ash particulates thereby and which will create the annular particle free volume 46 under the wall 48. An upwardly angled or inclined lower wall 50 provided with suitable perforations 52 is preferably joined to the upper wall 48 to support the latter and further define therewith the annular volume or void 46.
The partially gasified char, which still contains some carbon, and the ash as indicated by arrow 42 proceed downwardly through the moving bed 24 to locations in the lower portion of the moving bed disposed below the off-take 40 and towards a suitable perforated grate 54 supporting the moving bed 24. In this lower portion of the moving bed 24, the char is contacted with an oxidant (air or oxygen) and steam which are respectfully introduced into the lower region 26 through conduits 56 and 58.
This mixture of steam and oxidant passes upwardly through the perforations 60 in the grate 54 in a direction countercurrently to that of the char and ash in the downwardly moving bed. As a result of this countercurrent flow, the steam and oxidant contact the hot char and react with the residual carbon in the char to burn out carbon remaining in the char. The steam provides an additional source of heat for this reaction and also causes a steam-carbon reaction to occur which depletes the residual carbon in the char. This steam-carbon reaction effectively reduces the quantity of oxygen which would otherwise be needed to completely burn out the residual carbon in the char and increases the heating value of the fuel gas.The fuel gas formed in the lower portion of the moving bed are combined with the fuel gas produced in the upper portion of the moving bed by the downwardly flowing combustion gases and are withdrawn through the gas off-take line 40.
The ash resulting from these gasification procedures is discharged through the perforations 60 in the grate 54 and removed from the gasifier through a discharge port 62.
The gasification apparatus of the present invention provides a stream of hot fuel gas which is characterized by being essentially tar free and with a relatively low content of ammonia values. This essentially tar-free hot gas stream can be advantageously utilized in a gas turbine to extract the heat energy in the fuel gas since the gases discharged from the gasifier can be subject to particulate and sulfur removal procedures without excessively reducing the temperature of the gas stream. In order to further facilitate the reduction of sulfur species in the hot fuel gas, a sulfur sorbing material such as calcium carbonate may be injected into the gasifier along with the coal. Gasification rates may be enhanced by the addition of alkali catalysts to the coal feed to the gasifier.
Claims (12)
- Claim 1. A split-flow coal gasifier comprising an elongated vertically oriented reactor means having upper, lower and intermediate regions, means for introducing coal particulates including coal fines into said upper region to form a downwardly moving bed of coal particulates in said intermediate region, means for introducing a stream of combustion supporting medium into said upper region for effecting therein the combustion of said coal fines to provide a downwardly flowing stream of hot combustion gases contactable with downwardly moving coal particulates within an upper portion of said bed for reacting with the coal particulates therein to provide a stream of gaseous products including fuel gas while producing hot coal char and ash, means for introducing a gaseous oxidant and steam into said lower region for contacting and reacting with residual carbon in said char in said lower portion of the bed to provide a further stream of gaseous products including fuel gas, and discharge means in registry with said intermediate region and said bed at a location intermediate said upper portion and said lower portion for removing said streams of gaseous products from the reactor means.
- Claim 2. A split-flow coal gasifier as claimed in Claim 1, wherein the reaction of the combustion gases with the coal particulates in said upper portion of the bed releases tar and hydrocarbon values from the coal particulates, and wherein the tars and hydrocarbon values released from the coal are supported and conveyed by the first mentioned stream of gaseous products for contact with the hot coal char for sufficient heating thereof to substantially crack said tars and hydrocarbon values prior to the first mentioned stream of gaseous products reaching said discharge means.
- Claim 3. A split-flow coal gasifier as claimed in claim 1, wherein said discharge means includes gas off-take means and baffle means for directing solid particulate material away from said gas off-take means.
- Claim 4. A split-flow coal gasifier as claimed in claim 3, wherein said baffle means comprises annular inwardly inclined wall means for defining a gas-receiving annular volume, and wherein said gas off-take means is in registry with said annular volume for receiving gas therefrom.
- Claim 5. A split-flow coal gasifier as claimed in Claim 1, wherein said means for introducing coal particulates including coal fines comprises at least one conduit means in registry with said upper region.
- Claim 6. A split-flow coal gasifier as claimed in Claim 5, wherein the coal particulates are mixed with water and introduced into the upper region through said conduit means as a coal water slurry.
- Claim 7. A split-flow coal gasifier as claimed in Claim 5, wherein the coal fines comprise coal particulates of a size less than about 0.25 inch.
- Claim 8. A split-flow coal gasifier as claimed in Claim 7, wherein the coal fines comprise about 5 to 50 percent of the coal particulates.
- Claim 9. A split-flow coal gasifier as claimed in Claim 5, wherein said at least one conduit means comprise a plurality of conduit means, and wherein a stream substantially comprising coal fines is introduced into the upper region through at least one of said plurality of conduit means.
- Claim 10. A split-flow coal gasifier as claimed in Claim 9, wherein means are coupled to said at least one of said plurality of conduit means for introducing thereinto a stream of air for injecting the coal fines in said at least one of said plurality of conduit means into said upper region.
- Claim 11. A split-flow coal gasifier as claimed in Claim 5, wherein a further conduit means is in registry with said upper region for introducing thereinto a stream of steam.
- Claim 12. A split-flow coal gasifier as claimed in Claim 5, wherein said combustion supporting medium comprises air or oxygen, and wherein the concentration of air or oxygen is sufficient to provide near stoichiometric or sub-stoichiometric reaction conditions in said upper region.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US75806591A | 1991-09-12 | 1991-09-12 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| GB9218050D0 GB9218050D0 (en) | 1992-10-14 |
| GB2259521A true GB2259521A (en) | 1993-03-17 |
Family
ID=25050352
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB9218050A Withdrawn GB2259521A (en) | 1991-09-12 | 1992-08-25 | Moving bed coal gasifier |
Country Status (2)
| Country | Link |
|---|---|
| CA (1) | CA2077029A1 (en) |
| GB (1) | GB2259521A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0625562A1 (en) * | 1993-05-19 | 1994-11-23 | Hugo Petersen Ges. für verfahrenstechn. Anlagenbau mbH & Co KG | Process for gasification of solid substances and gasification reactor |
| CN102242003A (en) * | 2010-05-12 | 2011-11-16 | 武汉海德新能源投资有限公司 | Composite type oxygen-enriching biomass gasification furnace |
| EP2606105A2 (en) * | 2010-08-16 | 2013-06-26 | Energy & Environmental Research Center Foundation | Sandwich gasification process for high-efficiency conversion of carbonaceous fuels to clean syngas with zero residual carbon discharge |
| WO2015192931A1 (en) * | 2014-06-20 | 2015-12-23 | L'air Liquide Societe Anonyme Pour L'etude Et Sexploitation Des Procedes Georges Claude | Process for heating and gasifying a carbonaceous fuel |
| CN113390082A (en) * | 2021-05-31 | 2021-09-14 | 上海海琦环保科技有限公司 | Fixed bed continuous upper air suction furnace for waste treatment |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0051482A1 (en) * | 1980-11-04 | 1982-05-12 | Douglas Cochrane Sons And Company (Proprietary) Limited | Production of producer gas |
| GB2116201A (en) * | 1982-03-01 | 1983-09-21 | Skf Steel Eng Ab | Gasifying carbonacenous material |
| EP0240483A1 (en) * | 1986-04-01 | 1987-10-07 | DISTRIGAZ Société anonyme dite: | Process and apparatus for the concurrent gasification of coal |
-
1992
- 1992-08-25 GB GB9218050A patent/GB2259521A/en not_active Withdrawn
- 1992-08-27 CA CA002077029A patent/CA2077029A1/en not_active Abandoned
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0051482A1 (en) * | 1980-11-04 | 1982-05-12 | Douglas Cochrane Sons And Company (Proprietary) Limited | Production of producer gas |
| GB2116201A (en) * | 1982-03-01 | 1983-09-21 | Skf Steel Eng Ab | Gasifying carbonacenous material |
| EP0240483A1 (en) * | 1986-04-01 | 1987-10-07 | DISTRIGAZ Société anonyme dite: | Process and apparatus for the concurrent gasification of coal |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0625562A1 (en) * | 1993-05-19 | 1994-11-23 | Hugo Petersen Ges. für verfahrenstechn. Anlagenbau mbH & Co KG | Process for gasification of solid substances and gasification reactor |
| CN102242003A (en) * | 2010-05-12 | 2011-11-16 | 武汉海德新能源投资有限公司 | Composite type oxygen-enriching biomass gasification furnace |
| CN102242003B (en) * | 2010-05-12 | 2013-06-05 | 武汉海德新能源投资有限公司 | Composite type oxygen-enriching biomass gasification furnace |
| EP2606105A2 (en) * | 2010-08-16 | 2013-06-26 | Energy & Environmental Research Center Foundation | Sandwich gasification process for high-efficiency conversion of carbonaceous fuels to clean syngas with zero residual carbon discharge |
| EP2606105A4 (en) * | 2010-08-16 | 2014-08-27 | Energy & Environ Res Ct Found | Sandwich gasification process for high-efficiency conversion of carbonaceous fuels to clean syngas with zero residual carbon discharge |
| US10011792B2 (en) | 2010-08-16 | 2018-07-03 | Nikhil Manubhai Patel | Sandwich gasification process for high-efficiency conversion of carbonaceous fuels to clean syngas with zero residual carbon discharge |
| US10550343B2 (en) | 2010-08-16 | 2020-02-04 | Nikhil Manubhai Patel | Sandwich gasification process for high-efficiency conversion of carbonaceous fuels to clean syngas with zero residual carbon discharge |
| US11220641B2 (en) | 2010-08-16 | 2022-01-11 | Nikhil Manubhai Patel | Sandwich gasification process for high-efficiency conversion of carbonaceous fuels to clean syngas with zero residual carbon discharge |
| EP4148108A1 (en) * | 2010-08-16 | 2023-03-15 | Singularity Energy Technologies, LLC | Sandwich gasification process for high-efficiency conversion of carbonaceous fuels to clean syngas with zero residual carbon discharge |
| WO2015192931A1 (en) * | 2014-06-20 | 2015-12-23 | L'air Liquide Societe Anonyme Pour L'etude Et Sexploitation Des Procedes Georges Claude | Process for heating and gasifying a carbonaceous fuel |
| CN113390082A (en) * | 2021-05-31 | 2021-09-14 | 上海海琦环保科技有限公司 | Fixed bed continuous upper air suction furnace for waste treatment |
Also Published As
| Publication number | Publication date |
|---|---|
| CA2077029A1 (en) | 1993-03-13 |
| GB9218050D0 (en) | 1992-10-14 |
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