CA1288598C - Process for partial oxidation of a hydrocarbon-containing gel - Google Patents
Process for partial oxidation of a hydrocarbon-containing gelInfo
- Publication number
- CA1288598C CA1288598C CA000542144A CA542144A CA1288598C CA 1288598 C CA1288598 C CA 1288598C CA 000542144 A CA000542144 A CA 000542144A CA 542144 A CA542144 A CA 542144A CA 1288598 C CA1288598 C CA 1288598C
- Authority
- CA
- Canada
- Prior art keywords
- channel
- oxygen
- concentric
- fuel
- supplying
- 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 - Fee Related
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/36—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents
- C01B3/363—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents characterised by the burner used
-
- 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
-
- 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
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0959—Oxygen
-
- 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
- C10J2300/12—Heating the gasifier
- C10J2300/1223—Heating the gasifier by burners
-
- 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
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Inorganic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Hydrogen, Water And Hydrids (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
A B S T R A C T
PROCESS FOR PARTIAL OXIDATION OF
A HYDROCARBON-CONTAINING FUEL
Process for the partial oxidation of fuel using a multi-orifice burner comprising a central channel and three concentric channels encircling the central channel. Fuel is supplied through the second concentric channel at a specific velocity: oxygen is supplied through the other channels at specific mass flow distribution and velocities.
PROCESS FOR PARTIAL OXIDATION OF
A HYDROCARBON-CONTAINING FUEL
Process for the partial oxidation of fuel using a multi-orifice burner comprising a central channel and three concentric channels encircling the central channel. Fuel is supplied through the second concentric channel at a specific velocity: oxygen is supplied through the other channels at specific mass flow distribution and velocities.
Description
~3,5~
P~)CESS FOR PAR~rIAL 07~:DATION OF
A HYDROCARBON~NTAINI~'~G Ft~
The invention relates to a process for partial oxidation of a hydrocarbon-containing fuel using a multi-orifice burner.
In particular, the invention relates to a process for partial oxidation of a hydrocarbon-containing fuel wherein an oxygen-con-taining gas and a hydrocarbon-containing fuel are supplied to a gasification zone through a quadruple orifice burner comprising a concentric arrangement of 3 oxygen-passages or channels and l fuel passage or channel, and wherein autothermically a gaseous stream containing synthesis gas is produced under appropriate conditions.
The oxygen-con~aining gas is usually air or pure oxygen or a mixture thereof. In order to control the temperature in the gasifi-~ cation zone a moderator gas can be supplied to said zone.
;; In particular, the invention relates to a process as described in the foregoing, wherein a liquid is suitable as a fuel.
More in particular, (heavy~ residue feedstock is suitable to be used as a fuel.
In such processes it is necessary to ensure fine atomization of ~he fuel and good and rapid contacting or mixing of the fuel and the oxygen-containing gas in order to obtain an excellent gasi-fication process.
It is an object of the invention to provide a process forpartial oxidation of a hydrocarbon-containing fuel wherein in situ fine atomization of the fuel is obtained. It is another object of the invention to provide a process for partial oxidation of a hydrocarbon-containing fuel wherein a good and rapid mLxing or contacting of oxygen and fuel is obtained and pre-ignition or flame-flash-back is prevented.
It is another object of the invention to provide a process for (heavy) residue gasification wherein economic process conditions , ' :~, '` ' - ' ' .~ ' :
~ ~8B59~
(for example reduction of supply moderator gas and reduction of soot production) are achieved with a sufficiently long burner-lifetime (lon~er than 8000 operating hours).
The invention therefore provides a process for partial oxida-tion of a hydrocarbon-containing fuel characterized by the steps of supplying an oxygen-containing gas and hydrocarbon-containing fuel to a gasification zone through a concentric burner-arrangement of 3 oxygen passages or channels and 1 fuel passage or channel, and producing auto-thermically a gaseous stream containing synthesis gas under appropriate conditions, and further cc~prising the steps of supplying the oxygen-containing gas through the central channel of the concentric arrangement at a relatively low velocity of 21-42 mlsec; supplying oxygen-containing gas through the first concentric channel encircling the central channel at a relatively high veloci-ty of 60-120 m/sec; supplying fuel through the second concentric channel encircling the first channel at a relatively low velocity of 3.0-3.8 m/sec; and supplying oxygen-containing gas through the third concentric channel encircling the second channel at a relati-vely hign velocity of 60-120 m/sec.
In an advantageous embodi~ent of the invention 5 to 40 mass per cent of the oxygen-containing gas is supplied through the said central channel.
In another advantageous emkodiment of the invention the respective velocities are measured at the outlet of the said respective concentric channels into the gasification zone. The velocity measurement can be carried out in any way suitable for the purpose and will not be described in detail.
In still another advantageous e~bodiment of the invention the oxygen-containing gas contains steam or carbon dioxide as a modera-tor. In still another advantageous ~mbodiment of the invention thegasification process is carried out at a pressure of 0.1-12 MPa.
The fuel and the oxygen-containing gas are supplied to the gasification zone through a concentric burner-arrangement of 3 oxygen passages and 1 fuel passage. A central channel for oxygen supply is surrounded by a first annular channel for oxygen supply.
.
, , '' ~, `': `
~2~
The said first annular channel is surrounded by a second annular channe] for fuel supply and the said second channel is surrounded by a third annular channel for oxygen supply.
Multi-orifice burners ccmprising arrangements of annular concentric channels for supplying oxygen and fuel to gasification - zones are known as such and will not be described in detail.
According to the invention the oxygen and the fuel are sup-plied to the gasification zone through the respective channels at specific velocities in order to obtain a good atomization and mixing.
The invention will now b~ described in re ~etail by referen-- ce to the following example.
Example Tests have been carried out under the following conditions:
a) Feedstock specific gravity at 15 degr.C (kg/m~) 980-1018 viscosity at channel outlet (Pa.s) 0.02-0.2 composition C %wt 86.7 - 87.4 H 10.2 - 10.8 S 1.26 - 1.39 - ~ N 0.3 - 0.5 . .
~ ash 0.064 .
typical metal content V ppm 252 Ni pFm 82 ~` Fe ppm 27 conradson carbon residu %wt 23 b) oxygen ccmposition 2 %vol 99.05 N2 " O . 01 Ar "
-~ H2O " __ - .:
: ~ - `
. ~ ;~ . .
.
. . : . -: ,. '. ' ';, ' .
' '128B5~
c) Opera~ing conditions ~eedstock ~fuel) mass flow (kg/s) 1.1 - 1.4 supply temperature to channel (degr.C.) 120 - 170 supply pressure (MPa) 3.6 - 3.7 velocity at fuel channel outlet (m/s) 3.0 - 3.8 resulting slot width (mm) 3 oxygen containing gas oxygen to fuel ratio (kg/kg) 1.0 - 1.3 steam to fuel ratio (kg/kg) 0.3 - 0.65 supply temperature of mlxture (degr.C) 210 - 220 supply pressure (MPa) 3.6 - 3.7 Distribution of mass flcw and velocity central channel, 5-40 mass per cent 21 - 42 m/s first concentric channel 60 - 120 m/s third concentric channel 60 - 120 mls wherein the mass flows through the first and third channel are distributed in an even manner reactor pressure (MPa) 0.1 - 12 -temperature (degr.C.) 1300 - 1450 .
Typical crude syngas composition %vol dry C2 = 5.3 - 9.1 ~2S = 0.1 - 0.3 2 = 0.0 - 0.1 H2 = 44.7 - 47.5 N = 0.1 - 0.4 CO = 43.7 - 48.9 CH4 = 0.05 - 0.3 :, ~
' . ' , ,. :, , ' .. : . . :
~: , ,. : ' : ' '~ . :
. . .
, ~ 213~3S~
unconvertel carbon-containing producks ca 0.3~4~ by weight on Euel, may be added to the feedstock.
In an advantageous embodiment of the invention the burner-lifetime can be increased by supplying an inert gas (a gas w~ich does not react exothermically) such as H20, C02, CH4 and the like through a fourth concentric annular channel surrounding the third channel. In this nEu~ner flame-lifting can occ~r and the heat flux can decrease.
Various modifications of the present in~ention will beccme apparent to those skilled in the art frcm the foregoing descrip-tion. Such modifications are intended to fall within the scope of the appended claims.
: : . - -.
.. . : ': :''
P~)CESS FOR PAR~rIAL 07~:DATION OF
A HYDROCARBON~NTAINI~'~G Ft~
The invention relates to a process for partial oxidation of a hydrocarbon-containing fuel using a multi-orifice burner.
In particular, the invention relates to a process for partial oxidation of a hydrocarbon-containing fuel wherein an oxygen-con-taining gas and a hydrocarbon-containing fuel are supplied to a gasification zone through a quadruple orifice burner comprising a concentric arrangement of 3 oxygen-passages or channels and l fuel passage or channel, and wherein autothermically a gaseous stream containing synthesis gas is produced under appropriate conditions.
The oxygen-con~aining gas is usually air or pure oxygen or a mixture thereof. In order to control the temperature in the gasifi-~ cation zone a moderator gas can be supplied to said zone.
;; In particular, the invention relates to a process as described in the foregoing, wherein a liquid is suitable as a fuel.
More in particular, (heavy~ residue feedstock is suitable to be used as a fuel.
In such processes it is necessary to ensure fine atomization of ~he fuel and good and rapid contacting or mixing of the fuel and the oxygen-containing gas in order to obtain an excellent gasi-fication process.
It is an object of the invention to provide a process forpartial oxidation of a hydrocarbon-containing fuel wherein in situ fine atomization of the fuel is obtained. It is another object of the invention to provide a process for partial oxidation of a hydrocarbon-containing fuel wherein a good and rapid mLxing or contacting of oxygen and fuel is obtained and pre-ignition or flame-flash-back is prevented.
It is another object of the invention to provide a process for (heavy) residue gasification wherein economic process conditions , ' :~, '` ' - ' ' .~ ' :
~ ~8B59~
(for example reduction of supply moderator gas and reduction of soot production) are achieved with a sufficiently long burner-lifetime (lon~er than 8000 operating hours).
The invention therefore provides a process for partial oxida-tion of a hydrocarbon-containing fuel characterized by the steps of supplying an oxygen-containing gas and hydrocarbon-containing fuel to a gasification zone through a concentric burner-arrangement of 3 oxygen passages or channels and 1 fuel passage or channel, and producing auto-thermically a gaseous stream containing synthesis gas under appropriate conditions, and further cc~prising the steps of supplying the oxygen-containing gas through the central channel of the concentric arrangement at a relatively low velocity of 21-42 mlsec; supplying oxygen-containing gas through the first concentric channel encircling the central channel at a relatively high veloci-ty of 60-120 m/sec; supplying fuel through the second concentric channel encircling the first channel at a relatively low velocity of 3.0-3.8 m/sec; and supplying oxygen-containing gas through the third concentric channel encircling the second channel at a relati-vely hign velocity of 60-120 m/sec.
In an advantageous embodi~ent of the invention 5 to 40 mass per cent of the oxygen-containing gas is supplied through the said central channel.
In another advantageous emkodiment of the invention the respective velocities are measured at the outlet of the said respective concentric channels into the gasification zone. The velocity measurement can be carried out in any way suitable for the purpose and will not be described in detail.
In still another advantageous e~bodiment of the invention the oxygen-containing gas contains steam or carbon dioxide as a modera-tor. In still another advantageous ~mbodiment of the invention thegasification process is carried out at a pressure of 0.1-12 MPa.
The fuel and the oxygen-containing gas are supplied to the gasification zone through a concentric burner-arrangement of 3 oxygen passages and 1 fuel passage. A central channel for oxygen supply is surrounded by a first annular channel for oxygen supply.
.
, , '' ~, `': `
~2~
The said first annular channel is surrounded by a second annular channe] for fuel supply and the said second channel is surrounded by a third annular channel for oxygen supply.
Multi-orifice burners ccmprising arrangements of annular concentric channels for supplying oxygen and fuel to gasification - zones are known as such and will not be described in detail.
According to the invention the oxygen and the fuel are sup-plied to the gasification zone through the respective channels at specific velocities in order to obtain a good atomization and mixing.
The invention will now b~ described in re ~etail by referen-- ce to the following example.
Example Tests have been carried out under the following conditions:
a) Feedstock specific gravity at 15 degr.C (kg/m~) 980-1018 viscosity at channel outlet (Pa.s) 0.02-0.2 composition C %wt 86.7 - 87.4 H 10.2 - 10.8 S 1.26 - 1.39 - ~ N 0.3 - 0.5 . .
~ ash 0.064 .
typical metal content V ppm 252 Ni pFm 82 ~` Fe ppm 27 conradson carbon residu %wt 23 b) oxygen ccmposition 2 %vol 99.05 N2 " O . 01 Ar "
-~ H2O " __ - .:
: ~ - `
. ~ ;~ . .
.
. . : . -: ,. '. ' ';, ' .
' '128B5~
c) Opera~ing conditions ~eedstock ~fuel) mass flow (kg/s) 1.1 - 1.4 supply temperature to channel (degr.C.) 120 - 170 supply pressure (MPa) 3.6 - 3.7 velocity at fuel channel outlet (m/s) 3.0 - 3.8 resulting slot width (mm) 3 oxygen containing gas oxygen to fuel ratio (kg/kg) 1.0 - 1.3 steam to fuel ratio (kg/kg) 0.3 - 0.65 supply temperature of mlxture (degr.C) 210 - 220 supply pressure (MPa) 3.6 - 3.7 Distribution of mass flcw and velocity central channel, 5-40 mass per cent 21 - 42 m/s first concentric channel 60 - 120 m/s third concentric channel 60 - 120 mls wherein the mass flows through the first and third channel are distributed in an even manner reactor pressure (MPa) 0.1 - 12 -temperature (degr.C.) 1300 - 1450 .
Typical crude syngas composition %vol dry C2 = 5.3 - 9.1 ~2S = 0.1 - 0.3 2 = 0.0 - 0.1 H2 = 44.7 - 47.5 N = 0.1 - 0.4 CO = 43.7 - 48.9 CH4 = 0.05 - 0.3 :, ~
' . ' , ,. :, , ' .. : . . :
~: , ,. : ' : ' '~ . :
. . .
, ~ 213~3S~
unconvertel carbon-containing producks ca 0.3~4~ by weight on Euel, may be added to the feedstock.
In an advantageous embodiment of the invention the burner-lifetime can be increased by supplying an inert gas (a gas w~ich does not react exothermically) such as H20, C02, CH4 and the like through a fourth concentric annular channel surrounding the third channel. In this nEu~ner flame-lifting can occ~r and the heat flux can decrease.
Various modifications of the present in~ention will beccme apparent to those skilled in the art frcm the foregoing descrip-tion. Such modifications are intended to fall within the scope of the appended claims.
: : . - -.
.. . : ': :''
Claims (8)
1. A process for partial oxidation of a hydrocarbon-containing fuel characterized by the steps of supplying an oxygen-containing gas and hydrocarbon-containing fuel to a gasification zone through a concentric burner-arrangement of 3 oxygen passages or channels and 1 fuel passage or channel, and producing auto thermically a gaseous stream containing synthesis gas under appropriate conditions, and further comprising the steps of supplying the oxygen-containing gas through the central channel of the concentric arrangement at a relatively low velocity of 21-42 m/sec; supplying oxygen-containing gas through the first concentric channel encircling the central channel at a relatively high velocity of 60-120 m/sec; supplying fuel through the second concentric channel encircling the first channel at a relatively low velocity of 3.0-3.8 m/sec; and supplying oxygen-containing gas through the third concentric channel encircling the second channel at a relatively high velocity of 60-120 m/sec.
2. The process as claimed in claim 1 characterized in that the respective velocities are measured at the outlet of the said respective concentric channels into the gasification zone.
3. The process as claimed in claim 1 characterized in that the hydrocarbon-containing fuel is a liquid.
4. The process as claimed in claim 1, 2 or 3 characterized in that the oxygen containing gas contains a moderator.
5. The process as claimed in claim 1, 2 or 3 characterized in that the oxygen-containing gas contains a moderator that is steam or carbon dioxide.
6. The process as claimed in claim 1, 2 or 3 characterized in that the process is carried out at a pressure of 0.1-12 MPa.
7. The process as claimed in claim 1, 2 or 3 characterized in that 5 to 40 mass per cent of the oxygen-containing gas is supplied through the said central channel.
8. The process as claimed in claim 1, 2 or 3 characterized by the step of supplying an inert gas (a gas which does not react exothermically) through a fourth concentric channel encircling the said third channel.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB8619076 | 1986-08-05 | ||
| GB868619076A GB8619076D0 (en) | 1986-08-05 | 1986-08-05 | Partial oxidation of fuel |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1288598C true CA1288598C (en) | 1991-09-10 |
Family
ID=10602239
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000542144A Expired - Fee Related CA1288598C (en) | 1986-08-05 | 1987-07-15 | Process for partial oxidation of a hydrocarbon-containing gel |
Country Status (17)
| Country | Link |
|---|---|
| US (1) | US4789384A (en) |
| EP (1) | EP0255748B1 (en) |
| JP (1) | JP2587242B2 (en) |
| CN (1) | CN1006629B (en) |
| AU (1) | AU590106B2 (en) |
| BR (1) | BR8703954A (en) |
| CA (1) | CA1288598C (en) |
| CS (1) | CS265245B2 (en) |
| DD (1) | DD261350A5 (en) |
| DE (1) | DE3773791D1 (en) |
| ES (1) | ES2025139B3 (en) |
| GB (1) | GB8619076D0 (en) |
| IN (1) | IN169781B (en) |
| NO (1) | NO171011C (en) |
| PT (1) | PT85471B (en) |
| RU (1) | RU2039699C1 (en) |
| ZA (1) | ZA875721B (en) |
Families Citing this family (19)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4888031A (en) * | 1988-05-26 | 1989-12-19 | Shell Oil Company | Process for partial oxidation of a liquid or solid and/or a gaseous hydrocarbon-containing fuel |
| US5087271A (en) * | 1990-11-19 | 1992-02-11 | Texaco Inc. | Partial oxidation process |
| EP0595472B1 (en) * | 1992-10-22 | 1997-07-16 | Texaco Development Corporation | Environmentally acceptable process for disposing of scrap plastic materials |
| EG20966A (en) * | 1995-06-06 | 2000-07-30 | Shell Int Research | A method for flame stabilization in a process for preparing synthesis gas |
| US6245303B1 (en) | 1998-01-14 | 2001-06-12 | Arthur D. Little, Inc. | Reactor for producing hydrogen from hydrocarbon fuels |
| US6126908A (en) * | 1996-08-26 | 2000-10-03 | Arthur D. Little, Inc. | Method and apparatus for converting hydrocarbon fuel into hydrogen gas and carbon dioxide |
| US6269286B1 (en) * | 1998-09-17 | 2001-07-31 | Texaco Inc. | System and method for integrated gasification control |
| US6221280B1 (en) | 1998-10-19 | 2001-04-24 | Alliedsignal Inc. | Catalytic partial oxidation of hydrocarbon fuels to hydrogen and carbon monoxide |
| US6641625B1 (en) | 1999-05-03 | 2003-11-04 | Nuvera Fuel Cells, Inc. | Integrated hydrocarbon reforming system and controls |
| DE10200639A1 (en) * | 2002-01-10 | 2003-07-24 | Oxeno Olefinchemie Gmbh | Process for the production of synthesis gas |
| US6755355B2 (en) | 2002-04-18 | 2004-06-29 | Eastman Chemical Company | Coal gasification feed injector shield with integral corrosion barrier |
| US6892654B2 (en) * | 2002-04-18 | 2005-05-17 | Eastman Chemical Company | Coal gasification feed injector shield with oxidation-resistant insert |
| ITMI20041860A1 (en) * | 2004-09-30 | 2004-12-30 | Eni Spa | EQUIPMENT TO SPRAY A LIQUID CURRENT WITH A GASEY DISPERSING CURRENT AND MIX THE NEBULIZED PRODUCT WITH AN ADDITIONAL GASEOUS CURRENT SUITABLE FOR EQUIPMENT TO CARRY OUT PARTIAL CATALYTIC OXIDATIONS AND ITS PROCEEDS |
| AU2007274366B2 (en) * | 2006-07-11 | 2010-09-09 | Shell Internationale Research Maatschappij B.V. | Process to prepare a synthesis gas |
| US7569156B2 (en) * | 2006-07-14 | 2009-08-04 | Shell Oil Company | Process for the manufacture of synthesis gas by partial oxidation of a liquid hydrocarbon-containing fuel using a multi-orifice burner |
| ITMI20072228A1 (en) * | 2007-11-23 | 2009-05-24 | Eni Spa | PROCEDURE FOR PRODUCING SYNTHESIS AND HYDROGEN GAS STARTING FROM LIQUID AND GASEOUS HYDROCARBONS |
| EP2238223B1 (en) | 2008-01-28 | 2015-08-26 | Shell Internationale Research Maatschappij B.V. | Process to start-up a coal gasification reactor |
| BR112014001306A2 (en) * | 2011-07-29 | 2017-06-13 | Oxea Corp | improved oxo process and method for producing waste oil synthesis gas |
| CN105271115B (en) * | 2015-11-25 | 2018-06-26 | 华东理工大学 | A kind of gaseous hydrocarbons stove burner |
Family Cites Families (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR1073523A (en) * | 1900-01-01 | |||
| NL16272C (en) * | 1923-05-01 | |||
| AT369345B (en) * | 1973-05-08 | 1982-12-27 | Texaco Development Corp | METHOD FOR THE PRODUCTION OF SYNTHESIS GAS, REDUCING GAS OR HEATING GAS BY PARTIAL OXYDATION OF NORMALLY LIQUID HYDROCARBON |
| US4351647A (en) * | 1980-07-14 | 1982-09-28 | Texaco Inc. | Partial oxidation process |
| US4443228A (en) * | 1982-06-29 | 1984-04-17 | Texaco Inc. | Partial oxidation burner |
| EP0108427B1 (en) * | 1982-09-02 | 1986-10-22 | Shell Internationale Researchmaatschappij B.V. | Burner for the partial combustion of finely divided solid fuel |
| US4502633A (en) * | 1982-11-05 | 1985-03-05 | Eastman Kodak Company | Variable capacity gasification burner |
| US4493230A (en) * | 1983-01-24 | 1985-01-15 | Hughes Enoch A | Apparatus to open and close a meter ring |
| US4443230A (en) * | 1983-05-31 | 1984-04-17 | Texaco Inc. | Partial oxidation process for slurries of solid fuel |
| US4525175A (en) * | 1983-05-31 | 1985-06-25 | Texaco Inc. | High turn down burner for partial oxidation of slurries of solid fuel |
| GB8318195D0 (en) * | 1983-07-05 | 1983-08-03 | Shell Int Research | Burner |
| GB2151348B (en) * | 1983-12-09 | 1986-08-06 | Shell Int Research | Burner and process for producing synthesis gas from hydrocarbon fuel |
-
1986
- 1986-08-05 GB GB868619076A patent/GB8619076D0/en active Pending
-
1987
- 1987-07-15 CA CA000542144A patent/CA1288598C/en not_active Expired - Fee Related
- 1987-07-31 CN CN87105249A patent/CN1006629B/en not_active Expired
- 1987-08-03 PT PT85471A patent/PT85471B/en not_active IP Right Cessation
- 1987-08-03 BR BR8703954A patent/BR8703954A/en not_active IP Right Cessation
- 1987-08-03 EP EP87201472A patent/EP0255748B1/en not_active Expired - Lifetime
- 1987-08-03 IN IN557/MAS/87A patent/IN169781B/en unknown
- 1987-08-03 DE DE8787201472T patent/DE3773791D1/en not_active Expired - Fee Related
- 1987-08-03 NO NO873239A patent/NO171011C/en unknown
- 1987-08-03 AU AU76515/87A patent/AU590106B2/en not_active Ceased
- 1987-08-03 ES ES87201472T patent/ES2025139B3/en not_active Expired - Lifetime
- 1987-08-03 RU SU874203139A patent/RU2039699C1/en not_active IP Right Cessation
- 1987-08-03 ZA ZA875721A patent/ZA875721B/en unknown
- 1987-08-03 CS CS875779A patent/CS265245B2/en not_active IP Right Cessation
- 1987-08-03 DD DD87305654A patent/DD261350A5/en not_active IP Right Cessation
- 1987-08-03 JP JP62192771A patent/JP2587242B2/en not_active Expired - Fee Related
- 1987-08-04 US US07/081,504 patent/US4789384A/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| EP0255748B1 (en) | 1991-10-16 |
| BR8703954A (en) | 1988-04-05 |
| ES2025139B3 (en) | 1992-03-16 |
| CN87105249A (en) | 1988-02-17 |
| CN1006629B (en) | 1990-01-31 |
| JPS6343996A (en) | 1988-02-25 |
| JP2587242B2 (en) | 1997-03-05 |
| AU7651587A (en) | 1988-02-11 |
| GB8619076D0 (en) | 1986-09-17 |
| ZA875721B (en) | 1988-03-30 |
| CS265245B2 (en) | 1989-10-13 |
| AU590106B2 (en) | 1989-10-26 |
| DD261350A5 (en) | 1988-10-26 |
| PT85471A (en) | 1988-08-17 |
| NO171011B (en) | 1992-10-05 |
| PT85471B (en) | 1994-10-31 |
| IN169781B (en) | 1991-12-21 |
| NO171011C (en) | 1993-01-13 |
| CS577987A2 (en) | 1989-01-12 |
| US4789384A (en) | 1988-12-06 |
| DE3773791D1 (en) | 1991-11-21 |
| EP0255748A2 (en) | 1988-02-10 |
| NO873239D0 (en) | 1987-08-03 |
| NO873239L (en) | 1988-02-08 |
| EP0255748A3 (en) | 1988-09-07 |
| RU2039699C1 (en) | 1995-07-20 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKLA | Lapsed |