GB2233668A - Recovering heavy metal compounds - Google Patents
Recovering heavy metal compounds Download PDFInfo
- Publication number
- GB2233668A GB2233668A GB9013128A GB9013128A GB2233668A GB 2233668 A GB2233668 A GB 2233668A GB 9013128 A GB9013128 A GB 9013128A GB 9013128 A GB9013128 A GB 9013128A GB 2233668 A GB2233668 A GB 2233668A
- Authority
- GB
- United Kingdom
- Prior art keywords
- carbonaceous material
- heavy metal
- metal compounds
- furnace
- ash
- 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.)
- Granted
Links
- 229910001385 heavy metal Inorganic materials 0.000 title claims abstract description 15
- 150000002736 metal compounds Chemical class 0.000 title claims abstract description 15
- 238000000034 method Methods 0.000 claims abstract description 35
- 238000002485 combustion reaction Methods 0.000 claims abstract description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 9
- 238000011084 recovery Methods 0.000 claims abstract description 6
- 229910000831 Steel Inorganic materials 0.000 claims abstract description 3
- 239000010959 steel Substances 0.000 claims abstract description 3
- 239000003575 carbonaceous material Substances 0.000 claims description 21
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 17
- 239000007789 gas Substances 0.000 claims description 14
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 9
- 229910052799 carbon Inorganic materials 0.000 claims description 9
- 239000002245 particle Substances 0.000 claims description 9
- 238000007670 refining Methods 0.000 claims description 9
- 229910052759 nickel Inorganic materials 0.000 claims description 8
- 239000000567 combustion gas Substances 0.000 claims description 6
- 239000003921 oil Substances 0.000 claims description 5
- 239000011236 particulate material Substances 0.000 claims description 5
- 238000004140 cleaning Methods 0.000 claims description 3
- 239000003208 petroleum Substances 0.000 claims description 3
- 239000011819 refractory material Substances 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 2
- 238000000197 pyrolysis Methods 0.000 claims description 2
- 238000007790 scraping Methods 0.000 claims 1
- 150000003682 vanadium compounds Chemical class 0.000 claims 1
- 239000002006 petroleum coke Substances 0.000 abstract description 10
- 229910052720 vanadium Inorganic materials 0.000 abstract description 9
- 239000000571 coke Substances 0.000 abstract description 8
- 150000001875 compounds Chemical class 0.000 abstract description 8
- 239000002893 slag Substances 0.000 abstract description 8
- 238000000605 extraction Methods 0.000 abstract description 4
- 150000002816 nickel compounds Chemical class 0.000 abstract description 3
- 239000000843 powder Substances 0.000 abstract 1
- GPPXJZIENCGNKB-UHFFFAOYSA-N vanadium Chemical compound [V]#[V] GPPXJZIENCGNKB-UHFFFAOYSA-N 0.000 abstract 1
- 239000002956 ash Substances 0.000 description 10
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 description 10
- GNTDGMZSJNCJKK-UHFFFAOYSA-N divanadium pentaoxide Chemical compound O=[V](=O)O[V](=O)=O GNTDGMZSJNCJKK-UHFFFAOYSA-N 0.000 description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 239000000463 material Substances 0.000 description 6
- 229910002092 carbon dioxide Inorganic materials 0.000 description 5
- 239000000203 mixture Substances 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000010881 fly ash Substances 0.000 description 3
- 230000008018 melting Effects 0.000 description 3
- 238000002844 melting Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 230000002708 enhancing effect Effects 0.000 description 2
- 239000013618 particulate matter Substances 0.000 description 2
- HBMJWWWQQXIZIP-UHFFFAOYSA-N silicon carbide Chemical compound [Si+]#[C-] HBMJWWWQQXIZIP-UHFFFAOYSA-N 0.000 description 2
- 229910010271 silicon carbide Inorganic materials 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000003111 delayed effect Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 239000012717 electrostatic precipitator Substances 0.000 description 1
- 239000011152 fibreglass Substances 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 229910000765 intermetallic Inorganic materials 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G31/00—Compounds of vanadium
- C01G31/02—Oxides
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G53/00—Compounds of nickel
- C01G53/04—Oxides; Hydroxides
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C3/00—Combustion apparatus characterised by the shape of the combustion chamber
- F23C3/006—Combustion apparatus characterised by the shape of the combustion chamber the chamber being arranged for cyclonic combustion
- F23C3/008—Combustion apparatus characterised by the shape of the combustion chamber the chamber being arranged for cyclonic combustion for pulverulent fuel
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Inorganic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
Heavy metal compounds, particularly vanadium and nickel compounds are recovered from petroleum coke by combusting the coke under conditions constraining the temperatures to within the range 600 to 1400 DEG C, collecting the ash which is then subjected to a known process for the extraction of the metallic compounds. Whilst the combustion process may be achieved in a fluidised bed furnace, high recovery rates are likely to be achieved utilising a tubular furnace chamber 2 inclined at 10 DEG to horizontal. Dried petroleum coke, ground to fine powder (ASTM 75 micron, or less) is entrained into a primary air flow injected tangentially into the chamber through ports 18, 20, 22, 24 together with secondary air sufficient to maintain an oxidising atmosphere. Molten slag is deposited on the chamber wall by centrifugal action and drained from the chamber to fall on a rotating steel drum immersed in a water trough. A scraper removes the slag from the drum as flakes which are removed from the water trough using a screw conveyor.
Description
"PROCESS AND APPARATUS FOR RECOVERING HEAVY METAL
COMPOUNDS FROM CARBONACEOUS MATERIAL."
this invention relates to a process for recovering heavy metal compounds from carbonaceous material, and, more particularly, to a process for recovering vanadium and nickel compounds from petroleum coke.
In recent years a number of new processes have been developed for the refining of crude oil, and also for the further refining of residual oils remaining from primary refining processes, with the object of thus obtaining additional fractions and added value distillates not previously obtainable. These new processes, and particularly those which now convert the residuals from the traditional vacuum distillation processes into new and additional refinery products, also generate significant quantities of sub-products or refining residues commonLy known as "petroleum coke", "delayed coke", "fLex;-coke" and such like.These sub-products or refining residues vary widely in composition, the principal component invariably being carbon (C) with a secondary content of heavy metallic compounds such as oxides of vanadium (V) and nickel (Ni) varying in accordance with the composition of the petroleum oil being refined and also varying depending on the particular refining processes utilised.
In particular, it has been found that Venezuelan oils of all types have a relatively high, on a worldwide scale, content of both vanadium and nickel, and therefore both the fly-ash produced by burning the oil, for example in boilers supplying electric utilities, and the final petroleum coke residues from refining processes after gasification, are all relatively high in content of vanadium and nickel.
The metallic compounds or oxides of such vanadium and nickeL are intimately bound with the carbon in the petroleum coke and whilst they can be very effectively separated from the petroleum coke and also one from the other by acid-leaching and selective precipitation, that process is not economically practical for the extraction of vanadium and nickel from any of the various types of vanadium and nickel-bearing petroluem cokes presently being produced. The present invention is concerned with apparatus and a process to burn, oxidise or gasify the carbon content of the fly-ash or petroleum coke, and simultaneously to capture and recover the unburnable or non-volatile elements which constitute the ash.Upon converting the petroleum coke to ash, the metallic compounds form an appreciable proportion of the ash and the known processes for extraction of the metallic compounds may be exercised economically utilising the ash.
According to one aspect of the present invention there is provided a process for recovering heavy metal compounds from carbonaceous material including subjecting the carbonaceous material to pyrolysis in the presence of air combusting the carbon content at temperatures in the range of 6000to 14000C collecting the ash resuLting from combustion and subjecting the ash to a recovery process to separate the heavy metal compounds from the ash.
The heavy metal compounds may include vanadium and nickel and the carbonaceous material may be carbon contained in residues arising from refining processes for petroleum oils.
Preferably, the carbonaceous material is ground to a grain size to pass through 200 mesh American
Standard (ASTM 75 micron). An even finer particle size, that is down to pass through 325 mesh American
Standard (ASTM 45 micron) may, with advantage, be utiLised.
Desirably, the carbonaceous material is combusted at temperatures in excess of 6800C whilst upper temperatures of lower than 12000C or even 10000C are to be preferred.
Suitably, combustion is effected in a furnace of tubular form, having an open end, a closed end and a cylindrical wall, with ports for the carbonaceous material and combustion air arranged to discharge tangentially into the furnace, a combustion gas exit at the open end and a molten ash outlet draining to coLtection means. An inwardly directed throat may be provided adjacent the open end.
Alternatively, the combustion process is effected in a fluidised bed furnace.
Advantageously, the combustion gases are passed through a gas cleaning apparatus to recover particulate material therein which particulate material. is returned to the tubular furnace.
In one embodiment of the invention shown in the accompanying, partly diagrammatic, drawing the furnace 2 is of generally cylindrical form having an axis inclined at 100 to the horizontal and including an end plug 4, a frusto-conical portion 6 and a main cylindrical portion 8 provided with a throat 10 and a hot gas exit 12. The portions are formed as a water cooled shell 14 Lined with silicon carbide refractory material 16 and are penetrated by tangential feed ports 18, 20, 22, 24 - each divided into a radially outer secondary air port and a radially inner port for primary air and flexi-coke, a slag drain hole 26 and radial ports 28 for auxiliary gas firing. A slag outlet 30 leads to an extended, silicon carbide refractory lined, square cross-section, duct 32 discharging to a water trough (not shown) forming a gas seal.The molten slag is arranged to fall on to a steel roller immersed in the water to form thin flakes of solidified sLag which are scraped from the rotating roller and removed from the water trough by means of a screw conveyor (not shown) for treatment to extract the vanadium content.
The hot gas exit 12 is arranged to discharge to a chimney (not shown).
In operation, the furnace is fired such as to burn-off as effectively as possible the maximum carbon content of a metallic compound-bearing material such as coaL, fly-ash, petroleum coke, flexi-coke, or any similar material, whilst recovering the maximum amount possible of the resulting ash, which will contain a relatively high content of metallic compounds, and constitutes the final product.
The furnace is first pre-heated by injecting and igniting fuel utilising the auxiliary gas burner ports 28 until a temperature not less than six hundred degrees celsius (6000C) and up to one thousand two hundred degrees celsius (1,2000C) is achieved. At this point injection of the material to be combusted is commenced. The material should be dry, with a maximum of ten percent (10X) of humidity, and with a grain size of not more than an American Standard 40 mesh (ASTM 420 micron). Grain sizes of less than American Standard mesh 200 (ASTM 75 micron) and, preferably, Less than
American Standard mesh 325 (ASTM 45 micron) have been found to give enhanced results. The material to be combusted, for example flexi-coke, with a vanadium (V) content of between 2 percent and up to 10 percent is mixed with a quantity of primary air equivalent to approximately 15% of the flexi-coke stochiometric air requirement. This mixture is fed selectively to the furnace through the radially inner ports of the tangential feed-ports 18, 20, 22, 24 with feeding through the ports 20,24, tending to give best combustion results. Secondary combustion air is discharged through the radially outer ports of the feed ports 18, 20, 22, 24, to provide the required total excess air supply and to produce a strong rotating effect about the furnace axis.The ignited gas fuel-burners and radiant heat from the refractory walls causes the mixture to burn instantly with an extended dwell time in the chamber and flame temperature below 14000 celsius maximum and preferably below 12000 or even 10000 celsius. The centrifugal effect of the rotating flow urges the burning particles outwards so that the burning particles including vanadium pentoxide, with a melting point of approximately 680 degrees celsius, become semi-liquid and commence to adhere to the refractory walls 16 of the furnace, meanwhile the carbon particles continue to burn forming around the particles a protective bubble of carbon dioxide gas (C02), which inhibits further oxidation or burning.However, the rotating and violent swirling motion of the incandescent mass of particulate material within the furnace, combined with the resulting centrifugal force, produces a "scrubbing" around the interior of the refractory wall, continuously stripping away the combustion-inhibiting carbon dioxide on the walls, thus encouraging access of additional oxygen and the completion of the burning process, of any remaining unburnt carbon adhering to the walls 16 of the furnace.
The convergent effect of the throat 10, which reduces the cross-sectional diameter to approximately 40X of the diameter of the main cyLindricaL portion 8, produces an increase in rotational velocity of the gases about the central axis along the portion, thereby increasing the centrifugal forces acting on the slag particles and enhancing deposition of the particles on the refractory lining prior to discharge of the hot gas from the furnace as weL1 as increasing the dwell time o the particles in the chamber. However, in some instances, it may be found unnecessary to provide such a convergency and an exit aperture in an end wall may suffice.
The ash, deposited on the interior wall of the furnace at temperatures of approximately 1000 degrees celsius, will flow down the walls of the furnace, assisted by gravitational force, and will drain out of the furnace through the sLag drain holes 26 situated at the bottom of the furnace. Exit gases, mainly composed of carbon dioxide gas (CO2), are discharged through a chimney (not shown).Alternatively, if required, the exit gases may be cooled and subjected to extraction of any residual particulate matter by conventionaL means which incLude cyclones, electro-static precipitators, wet-scrubbers, fibreglass filters, andlor any other conventional gas-cleaning methods, the particulate matter recovered by such methods being subsequently re-circulated through the furnace for recuperation of the metallic compounds contained in such recuperated material thus enhancing the total recuperation of the metaLLic compounds by this process.
It will be appreciated that other orientations of the central axis of the furnace chamber may be utilised and, indeed, the furnace chamber may be orientated adjustably in any position from having the central axis extending horizontally to having the central axis extending vertically.
Since vanadium pentoxide (V205) has a melting point of approximately 650 degrees celsius whilst the lower oxides have melting points of approximately 1800 degrees celsius, a sufficient excess of air is required to minimise the formation of the lower oxides. In addition, since vanadium pentoxide is volatile, it is desirable to restrict the temperatures achieved in the furnace as much as possible whilst maintaining combustion. Temperatures of 1000, or up to 1200, degrees celsius have been found to avoid appreciable volatisation of the vanadium pentoxide in the furnace chamber.
It wiLL be appreciated that where recovery of nickel compounds is concerned, different temperature considerations may arise.
Claims (19)
1. A process for recovering heavy metal compounds from carbonaceous material including subjecting the carbonaceous material to pyrolysis in the presence of air to combust the carbon content at temperatures in the range of 6000C to 1400or and collecting ash resulting from combustion and subjecting the ash to a recovery process to separate the heavy metal compounds from the ash.
2. A process as claimed in CLaim 1, wherein the heavy metal compounds include vanadium compounds.
3. A process as claimed in CLaim 1 or Claim 2, wherein the heavy metal compounds include nickel.
4. A process as claimed in any preceding Claim, wherein the carbonaceous material is combusted at temperatures in excess of 6800C.
5. A process as claimed in any preceding Claim, wherein the carbonaceous material is initiaLLy ground to have a grain size to pass through 40 mesh American
Standard (ASTM 420 micron).
6. A process as claimed in any one of CLaims 1 to 4, wherein the carbonaceous material is ground to have a grain size to pass through 200 mesh American Standard (ASTM 75 micron).
7. A process as claimed in any one of Claims 1 to 4, wherein the carbonaceous material is ground to have a grain size to pass through 325 mesh American Standard (ASTM 45 micron).
8. A process as claimed in any preceding Claim, wherein the carbonaceous material is contained in residue arising from refining processes for petroleum oils.
9. A process as claimed in any preceding Claim, wherein the carbonaceous material is initially dried to have a moisture content of less than 10X.
10. A process as claimed in any preceding Claim, wherein combustion is effected in a furnace of tubular form, having an open end, a closed end and a cylindrical wall, with burner and combustion air ports arranged to discharge tangentially into the furnace, a combustion gas exit at the open end and a molten ash outlet draining to collection means.
11. A process as claimed in CLaim 10, wherein an inwardly directed throat is provided adjacent the open end.
12. A process as claimed in Claim 10 or Claim 11 wherein the tubular furnace is arranged with the major longitudinal axis extending at an inclination of 10 to the horizontal.
13. A process as claimed in one of Claims 1 to 9, wherein combustion is effected in a fluidized bed furnace, the carbonaceous material being injected into the bed to produce combustion gases and the ash being separated from the bed particles.
14. A process as claimed in CLaim 10, Claim 11, Claim 12 or Claim 13, wherein the combustion gases are passed through a gas cleaning apparatus to recover particulate material therein, which particulate material is returned to the furnace.
15. Apparatus for the recovery of heavy metal compounds from carbonaceous material including a tubular combustion furnace chamber having a wall lined with refractory material and provided with a water cooled jacket, the furnace chamber being substantially closed at one end and provided with an inwardly directed restricted throat outlet of refractory material at the other end, a series of axiaLLy spaced tangential ports positioned in the wall adjacent the throat outlet arranged to discharge combustion air and finely ground carbonaceous material containing heavy metal compounds tangentially into the furnace chamber, a molten ash outlet discharging on to a rotatable steel roller immersed in a water trough and means for scraping solidified ash as flakes from the surface of the roller and further. means for removing the fLakes of solidified ash from the water trough.
16. Apparatus as claimed in CLaim 15, wherein the major longitudinal axis of the tubular furnace chamber is inclined at approximately 100 to the horizontal.
17. Apparatus as claimed in CLaim 15 or Claim 16, wherein the furnace chamber is connected to discharge combustion gases through the restricted throat outlet directly to a chimney flue.
18. A process for recovering heavy metal compounds from carbonaceous material substantially as hereinbefore described with reference to the accompanying drawing.
19. Apparatus for the recovery of heavy metaL compounds from carbonaceous material arranged and adapted to operate substantially as hereinbefore described with reference to the accompanying drawing.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB898913565A GB8913565D0 (en) | 1989-06-13 | 1989-06-13 | Process for recovering heavy metal compounds from carbonaceous material |
Publications (3)
| Publication Number | Publication Date |
|---|---|
| GB9013128D0 GB9013128D0 (en) | 1990-08-01 |
| GB2233668A true GB2233668A (en) | 1991-01-16 |
| GB2233668B GB2233668B (en) | 1993-12-01 |
Family
ID=10658358
Family Applications (2)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB898913565A Pending GB8913565D0 (en) | 1989-06-13 | 1989-06-13 | Process for recovering heavy metal compounds from carbonaceous material |
| GB9013128A Expired - Fee Related GB2233668B (en) | 1989-06-13 | 1990-06-12 | Process and apparatus for recovering heavy metal compounds from carbonaceous material |
Family Applications Before (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB898913565A Pending GB8913565D0 (en) | 1989-06-13 | 1989-06-13 | Process for recovering heavy metal compounds from carbonaceous material |
Country Status (2)
| Country | Link |
|---|---|
| GB (2) | GB8913565D0 (en) |
| NL (1) | NL9001339A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0937944A3 (en) * | 1998-02-18 | 2000-01-05 | Loesche Gmbh | Combustion method and device for vanadium containing fuels |
| DE102007010776A1 (en) * | 2007-03-06 | 2008-09-11 | Gfe Metalle Und Materialien Gmbh | Process for the preparation of a heavy metal enriched, low-carbon concentrate from carbon-rich, heavy metal-containing residues, in particular petroleum processing |
| US8006407B2 (en) * | 2007-12-12 | 2011-08-30 | Richard Anderson | Drying system and method of using same |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4243639A (en) * | 1979-05-10 | 1981-01-06 | Tosco Corporation | Method for recovering vanadium from petroleum coke |
| US4389378A (en) * | 1980-10-20 | 1983-06-21 | Gulf Canada Limited | Process using sulphate reagent for recovering vanadium from cokes derived from heavy oils |
| US4705539A (en) * | 1985-12-02 | 1987-11-10 | Texaco Inc. | Partial oxidation process |
| US4788003A (en) * | 1985-06-27 | 1988-11-29 | Texaco Inc. | Partial oxidation of ash-containing liquid hydrocarbonaceous and solid carbonaceous |
| US4803061A (en) * | 1986-12-29 | 1989-02-07 | Texaco Inc. | Partial oxidation process with magnetic separation of the ground slag |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4217132A (en) * | 1977-09-27 | 1980-08-12 | Trw Inc. | Method for in-flight combustion of carbonaceous fuels |
-
1989
- 1989-06-13 GB GB898913565A patent/GB8913565D0/en active Pending
-
1990
- 1990-06-12 GB GB9013128A patent/GB2233668B/en not_active Expired - Fee Related
- 1990-06-13 NL NL9001339A patent/NL9001339A/en not_active Application Discontinuation
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4243639A (en) * | 1979-05-10 | 1981-01-06 | Tosco Corporation | Method for recovering vanadium from petroleum coke |
| US4389378A (en) * | 1980-10-20 | 1983-06-21 | Gulf Canada Limited | Process using sulphate reagent for recovering vanadium from cokes derived from heavy oils |
| US4788003A (en) * | 1985-06-27 | 1988-11-29 | Texaco Inc. | Partial oxidation of ash-containing liquid hydrocarbonaceous and solid carbonaceous |
| US4705539A (en) * | 1985-12-02 | 1987-11-10 | Texaco Inc. | Partial oxidation process |
| US4803061A (en) * | 1986-12-29 | 1989-02-07 | Texaco Inc. | Partial oxidation process with magnetic separation of the ground slag |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0937944A3 (en) * | 1998-02-18 | 2000-01-05 | Loesche Gmbh | Combustion method and device for vanadium containing fuels |
| DE102007010776A1 (en) * | 2007-03-06 | 2008-09-11 | Gfe Metalle Und Materialien Gmbh | Process for the preparation of a heavy metal enriched, low-carbon concentrate from carbon-rich, heavy metal-containing residues, in particular petroleum processing |
| DE102007010776B4 (en) * | 2007-03-06 | 2008-11-13 | Gfe Metalle Und Materialien Gmbh | Process for the preparation of a heavy metal enriched, low-carbon concentrate from carbon-rich, heavy metal-containing residues, in particular petroleum processing |
| US8006407B2 (en) * | 2007-12-12 | 2011-08-30 | Richard Anderson | Drying system and method of using same |
Also Published As
| Publication number | Publication date |
|---|---|
| GB8913565D0 (en) | 1989-08-02 |
| GB9013128D0 (en) | 1990-08-01 |
| NL9001339A (en) | 1991-01-02 |
| GB2233668B (en) | 1993-12-01 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PCNP | Patent ceased through non-payment of renewal fee |
Effective date: 19970612 |