CA2195554C - A process for the manufacture of synthesis gas by partial oxidation of a gaseous hydrocarbon-containing fuel using a multi-orifice (co-annular) burner - Google Patents
A process for the manufacture of synthesis gas by partial oxidation of a gaseous hydrocarbon-containing fuel using a multi-orifice (co-annular) burner Download PDFInfo
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- CA2195554C CA2195554C CA002195554A CA2195554A CA2195554C CA 2195554 C CA2195554 C CA 2195554C CA 002195554 A CA002195554 A CA 002195554A CA 2195554 A CA2195554 A CA 2195554A CA 2195554 C CA2195554 C CA 2195554C
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- 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
Abstract
A process for the manufacture of synthesis gas by reacting oxygen-containing gas, applied as oxidiser and gaseous hydrocarbon-containing fuel in a reaction zone of a non-catalytic gas generator comprising the step s of injecting the said fuel and the said oxidiser into the reaction zone through a multi-orifice (co-annular) burner comprising arrangement of n separate passages or channels coaxial with the Longitudinal axis of said burner, wherein n is an integer .gtoreq. 2 (2, 3, 4, 5...) wherein the (n-1)th passage is the inner passage with respect to the n th passage, measured from the longitudinal axis of the said burner, an d wherein geseous hydrocarbon-containing fuel and, optionally, a moderator is passed through one or more of the passages, but at least throug h the n th (outer) passage whereby at least one passage remains; oxidiser and, optionally, a moderator, is passed through one or more of the remaining passages, but at least through the (n-1)th, passage. In any two adjacent passages in which oxidiser is passed through the one passag e, and gaseous hydrocarbon-containing fuel is passed through the other passage, the said oxidiser has a higher velocity than said hydrocarbon-containing fuel.
Description
W O 96!03345 PCT/EP95/02877 a:~~~~il r ~ 2195554 y A PROCESS FOR THE MANUFACTURE OF SYNTHESIS GAS
BY PARTIAL OXIDATION OF A GASEOUS HYDROCARBON-CONTAINING
FUEL USING A MULTI-ORIFICE (CO-ANNULAR) BURNER
The invention relates to a process for the manufacture of synthesis gas by partial oxidation of a gaseous hydrocarbon-containing fuel using a multi-orifice (co-annular) burner.
In particular, the invention relates to a process for partial oxidation of a gaseous hydrocarbon-containing fuel wherein an oxygen-containing gas, which is applied as an oxidiser, and a gaseous hydrocarbon-containing fuel are supplied to a gasification zone through a multi-orifice (co-annular) burner comprising a concentric arrangement of n passages or channels coaxial with the longitudinal axis of said burner, wherein n is an integer _> 2, and wherein autothermically a gaseous stream containing synthesis gas is produced under appropriate conditions.
The oxygen-containing gas, which is applied as an oxidiser, is usually air or (pure) oxygen or steam or.a mixture thereof. In order to control the temperature in the gasification zone a moderator gas (for example steam, water or carbon dioxide or a-combination thereof) can be supplied to said zone.
Those skilled in the art will know the conditions of applying oxidiser and moderator.
Synthesis gas is a gas comprising carbon monoxide and hydrogen, and it is used, for example, as a clean medium-calorific value fuel gas or as a feedstock for the synthesis of methanol, ammonia or hydrocarbons, which latter synthesis yields gaseous hydrocarbons and liquid hydrocarbons such as gasoline, middle distillates, lub oils and waxes.
In the specification and in the claims the term gaseous hydrocarbon-containing fuel will be used to refer to hydrocarbon-containing fuel that is gaseous at gasifier feed pressure and temperature.
WO 96103345 PC1'IEP95I02877 'a''~' f ~. _ 2 _ 2 i 95554 According to an established process, synthesis gas is produced by partially oxidising in a reactor vessel a gaseous fuel such as gaseous hydrocarbon, in particular petroleum gas or natural gas, at a temperature in the range of from 1000 °C to 1800 °C and at a pressure in the range of from 0.1 MPa to 6 MPa abs. With the use of an oxygen containing gas.
Synthesis gas will often be produced near or at a crude oil refinery because the produced synthesis gas can directly be applied as a feedstock for the production of middle distillates, ammonia, hydrogen, methanol or as a fuel gas, for example, for heating the furnaces of the refinery or more efficiently for the firing of gas turbines to produce electricity and heat.
In co-annular (multi-orifice)- gas burners it has appeared that the burner lifetime is restricted by phenomena of pre-ignition or flame-flashback. Because of such phenomena the temperature of the burnez-internals becomes too high and serious burner damage will occur. Further, there are problems with corrosion of the gas burner tips.
It is an object of-the..invention.to-provide a process for partial oxidation of a gaseous hydrocarbon-containing fuel wherein a good and rapid mixing or contacting of oxygen-containing gas (oxidiser), fuel and, optionally, moderator gas in the gasification zone is achieved beyond the exit of the burner and wherein burner-damage by corrosion, pre-ignition or flame-flash-back is suppressed.
The invention solves the above burner damage problem in that in the process of the invention the oxygen-containing gas applied as oxidiser and the gaseous hydrocarbon-containing fuel are supplied to the gasification zone through specific passages at specific velocities.
The invention therefore provides a process for the manufacture of synthesis gas by reacting oxygen-containing gas, applied as oxidiser, and gaseous hydrocarbon-containing fuel in a reaction zone of a substantially non-catalytic gas genera~ot comprising the steps of injecting the said fuel and the said oxidiser into the reaction zone through a multi-orifice ico-annular) burner comprising an arrangement of n separate passages or channels coaxial with the longitudinal axis of said burner, wherein n is an integer _> 2 (2, 3, 4, 5 ...), wherein the (n-1)th passage is the inner passage with respect to the nth passage, measured from the longitudinal axis of the said burner, and wherein the said gaseous hydrocarbon-containing fuel (optionally with a moderator gas) is passed through one or more of the passages, but at least through the nth passage, whereby at least one passage remains; the said oxidiser (optionally with a moderator gas) is passed through one or more of the remaining passages, but at least through the (n-1)th passage, and in such a manner that in any two adjacent passages in Which oxidiser is passed through the one passage, and gaseous hydrocarbon-containing fuel is passed through the other passage, the said oxidiser has a higher velocity than said hydrocarbon-containing fuel, and provided that when n is 4, then all four passages are used.
In this manner the oxygen-containing gas (oxidiser) entrains the gaseous hydrocarbon-containing fuel after which the partial oxidation takes place in the gasification zone, and the burner-internal blades that form the internal separation wall between the oxygen-containing gas (oxidiser) and the hydrocarbon-containing gas and which have a finite thickness, are cooled by the oxygen-containing gas (oxidiser) and the hydrocarbon-containing gas (in particular by connective cooling) to lower the flame temperature just behind the tips.
Behind the tip of the blade there is unavoidably at least a recirculation area in which both gaseous fuel and oxygen-containing gas, applied as oxidiser, are present.
If the hydrocarbon-containing gas would have the highest velocity, there will be oxygen-rich conditions at the burner-internal-tip by means of "entrainment" which will lead to high flame temperatures, high tip temperatures and serious loss of burner material.
If the oxygen-containing gas, applied as oxidiser, has the highest velocity, in the recirculation area there will be mainly oxygen-depleted conditions, which will lead to lower flame temperature. Thus, serious burner damage will not occur, which leads i.,;;~,,,;
', ;' ;', ,',' ' ~~v.
- 4 _ ~' 95554 to a long burner-lifetime.
Advantageously, for n 2 3, at least part (e.g. 20$) of the gaseous hydrocarbon-containing fuel is passed through the said nth passage and the remainder of the gaseous hydrocarbon-containing fuel is passed through one or more of the remaining passages. The ( velocity of the oxygen-containing gas, applied as oxidiser, is advantageously 20-150 m/s.
The velocity of the gaseous hydrocarbon-containing fuel is advantageously 0.2-0.8 times the velocity of the oxygen-containing gas, applied as oxidiser, in any two adjacent passages in which oxidiser is passed through the one passage, and gaseous hydrocarbon-containing fuel is-passed through the other passage.
In an advantageous embodiment pf the invention the respective velocities are measured or calculated at the outlet of-the said respective channels into the gasification zone. The velocity measurement or calculation can be carried out by those skilled in the art in any way suitable for the purpose and will therefore not be described in detail. -In another-advantageous embodiment of the invention-the moderator gas is steam and/or water and/or carbon dioxide and the oxidiser contains at least 90$ pure 02. In-still anothei advantageous embodiment of the invention the gasification process is carried out at a pressure of-.0_1-12 MPa abs.
Multi-orifice burners comprising arrangements of annular , concentric channels for supplying oxygen-containing gas (oxidiser), fuel and moderator gas to a gasification zone are known as such (vide e.9. EP-A-0,545,281 and DE-OS-2,935,754) and the mechanical structures thereof--will therefore not be described in detail.-Usually such burners comprise a number of slits at the burner outlet and hollow-wall members with internal cooling fluid (e. g.
water) passages. The passages may or may not be converging at the burner outlet. Instead of comprising internal cooling fluid passages, the burner may be provided with a suitable ceramic or refractory lining applied onto or suspended by a means closely adjacent to the outer surface of the burner (front) wall for W096103345 _.. __ _ _ PGTYEP95I02877 y.a :. ! .5 ~: ~ 195554 -5_ resisting the heat load during operation or heat-up/shut down situations of the burner.
y No fuel passage is reserved for a fuel other than gaseous hydrocarbon-containing fuel.
The invention will now be described in moze detail by reference to the following examples.
A number of examples are given in the Table. In this Table the following abbreviations are made:
Feed l:Natural Gas with the following typical composition CHq : 94.4$ by volume C2H6 . 3.0$
C3H8 . 0.5$
C4H10 : 0.2$
CSH12+: 0.2$
. C02 . 0.29 N2 . 1.5$
The supply temperature to the burner.of this feedstock is 150-2so ac.
Feed 2: Natural Gas with the following typical composition CH4 : 81.8$ by volume C2H6 . 2.7$
C3H8 . 0.4$
C4H10 : O.I$
CSH12+: 0.1$
_Cp2 . 0.9$
N2 : 14.0$
C02._is supplied as a moderator gas to the said natural gas in such a manner that the mass ratio of moderator gas C02 to Natural Gas is 0.6-0.8. The supply temperature to the burner of this feedstock is 280-320 °C~-_ oxidiser l: 99.5$ pure 02 with a temperature of 230-250 °C.
oxidiser 2: a mixture of a gas with 99.5$ pure 02 with 20-30$ (by mass) of moderator gas. This mixture has a temperature of 250-270 °C
and the moderator gas is steam at a temperature of 280-300 °C.
r.: 2 i 95554 ~,'- ~ ,~ ,~, ;. : .,;
A number of 9 examples has been presented. The following Table indicates the distributions of the respective fuels and oxidisers for these examples. The typical synthesis gas compositions are also given. The values of n as used in the description and claims are indicated and passage 1 is the first-or central passage. !
r ~(~'~r'~' t 2.1.95 ~ ~.4 _,_ Table With Examples Exam 1e number 1 2 g Value of n 7 6 6 'S Typical synthesis gas composition -3 -7 -3 CO [8 Vol, dr ]
CO [B Vol, dr ] 34-35 39-40 34-35 i H [8 Vol, dr ] 62-63 47-48 62-63 Reactor ressura [MPa]9-5 2-3 5-, Reactor temperature Ide CI 300-1400 250-1350 300-1400 Passa a 1 T a of feed 1 oxidiser oxidiser 1 as 1 Mass flow [k /s] 1-1.5 1.2-1.8 1-1.5 i Velocit [m/s] 30-45 80-120 50-75 Passa a 2 T a of oxidiser feed 2 feed 1 as 1 Mass flow jk Js) 2.6-4 0.9-0.6 1.1-1.6 i Velocit [m/s] BO-120 30-45 25-35 - Passa a 3 T a of feed 1 feed 2 oxidiser 1 as Mass flow [k /s] 2.1-3.1 2.1-3.1 2-3 Velocit [m/s] 30-45 80-120 50-75 Passa a 4 T a of oxidiser feed 2 feed 1 1 as 1 Mass flow [k /s] 2.7-4 0.6-0.9 1.8-2.7 Velocit [m/s] 80-120 30-45 25-35 Passa a S T a of feed 1 oxidiser oxidiser 1 as 1 .
Mass flow [k /s] 2.1-3.1 1.2-1.8 2-3 Velocit [m/s] 30-45 80-120 50-75 Passa a 6 T a of oxidiser feed 2 feed 1 as 1 f Mass flow [k /s] 3-4.5 0.76-1.1 1-1.5 Velocit [m/s] 80-120 30-45 20-30 ) Passa a 7 T a of feed 1 as Mass flow (k /s1 1-1.5 Velocit [m/s] 30-45 ~ic~=~t ~:~. ; ,_ -8_ Table With Examples (Continued) Exam 1e aumber 4 S 6 Value of n 5 4 3 Typical synthesis gas composition -10 -5 -5 CO [~ Vol, dr ]
CO [8 Vol, dr ] 36-37 32-33 32-33 H [fl Vol, dr ] 47-48 62-63 62-63 Reactor ressure [MPa]2-3 I-1.5 2-3 Reactor temperature [de C] 1200-1300 1300-1400 1300-1400 Passa a 1 T a of as feed 2 feed 1 feed 1 Mass flow [k /s] 1-1.5 - 2-3 0.7-1.1 Velocit [m/sj 40-60 80-120- 45-80 Passa a 2 T a of as oxidiser.2 feed 1 oxidiser 1 Mass flow (k /s] 1.6-2.4 0.6-0.9 1.7-2.6 Velocit [m/s] 95-140 30-45 100-150 Passa a 3 T a of as feed 2 oxidiser feed 1 Mass flow [k /s] 2-3 6.2-9.3 0.9-1.3 Velocit [m/s] 40-60 80-120 35-40 Passa a 4. T a of oxidiser feed 1 moderator as as 2 Mass flow (k /s] 1.6-2.4 1.3-2 0.6-0.9 Velocit [m/s] 70-100 25-35 55-80 Passa a 5 T a of as feed 2 Mass flow [k /s] 1-1.5 Velocit (m/s] 30-45 '~'~~Vr~~ i 4~ _ g _ ~~~~554 Table With Examples (Continued) Exam 1e number 7 8 g Value of n 3 3 2 3 Typical synthesis gas composition -5 -3 -5 CO [8 Vol, dr ]
CO [8 Vol, dr ] 32-33 34-35 32-33 H [6 Vol, dr ] 62-63 62-63 62-63 Reactor ressure [MPa]2-3 4-5 7-10 Reactor temperature [de C] 1300-1400 1300-1400 1300-1400 Passa a 1 T a of as oxidiser feed 1 oxidiser 2 Mass flow [k /s] 2.5-3.5 2-3 6-8 Velocit [m/s] 40-60 40-70 95-60 .
Passa a 2 T a of as oxidiser oxidiser feed 1 Mass flow [k /s] 1.7-2.6 4-6 4-5.6 Velocit [m/s] 100-150 80-120 25-35 Passa a 3 T a of as feed 1 feed 1 Mass flow [k /s] 2.5-3.7 1.3-2 Velocit [m/s] 30-45 30-45 It will.be appreciated by those skilled in the art that any slit width suitable for the purpose can be applied, dependent on the burner capacity.
Advantageously, the first or central passage has a diameter up to 70 mm, whereas the remaining concentric passages have slit widths in the range of 1-20 mm.
Various modifications of the present invention will become apparent to those skilled in the art from the foregoing description.
Such modifications are intended to fall within the scope of the appended claims.
BY PARTIAL OXIDATION OF A GASEOUS HYDROCARBON-CONTAINING
FUEL USING A MULTI-ORIFICE (CO-ANNULAR) BURNER
The invention relates to a process for the manufacture of synthesis gas by partial oxidation of a gaseous hydrocarbon-containing fuel using a multi-orifice (co-annular) burner.
In particular, the invention relates to a process for partial oxidation of a gaseous hydrocarbon-containing fuel wherein an oxygen-containing gas, which is applied as an oxidiser, and a gaseous hydrocarbon-containing fuel are supplied to a gasification zone through a multi-orifice (co-annular) burner comprising a concentric arrangement of n passages or channels coaxial with the longitudinal axis of said burner, wherein n is an integer _> 2, and wherein autothermically a gaseous stream containing synthesis gas is produced under appropriate conditions.
The oxygen-containing gas, which is applied as an oxidiser, is usually air or (pure) oxygen or steam or.a mixture thereof. In order to control the temperature in the gasification zone a moderator gas (for example steam, water or carbon dioxide or a-combination thereof) can be supplied to said zone.
Those skilled in the art will know the conditions of applying oxidiser and moderator.
Synthesis gas is a gas comprising carbon monoxide and hydrogen, and it is used, for example, as a clean medium-calorific value fuel gas or as a feedstock for the synthesis of methanol, ammonia or hydrocarbons, which latter synthesis yields gaseous hydrocarbons and liquid hydrocarbons such as gasoline, middle distillates, lub oils and waxes.
In the specification and in the claims the term gaseous hydrocarbon-containing fuel will be used to refer to hydrocarbon-containing fuel that is gaseous at gasifier feed pressure and temperature.
WO 96103345 PC1'IEP95I02877 'a''~' f ~. _ 2 _ 2 i 95554 According to an established process, synthesis gas is produced by partially oxidising in a reactor vessel a gaseous fuel such as gaseous hydrocarbon, in particular petroleum gas or natural gas, at a temperature in the range of from 1000 °C to 1800 °C and at a pressure in the range of from 0.1 MPa to 6 MPa abs. With the use of an oxygen containing gas.
Synthesis gas will often be produced near or at a crude oil refinery because the produced synthesis gas can directly be applied as a feedstock for the production of middle distillates, ammonia, hydrogen, methanol or as a fuel gas, for example, for heating the furnaces of the refinery or more efficiently for the firing of gas turbines to produce electricity and heat.
In co-annular (multi-orifice)- gas burners it has appeared that the burner lifetime is restricted by phenomena of pre-ignition or flame-flashback. Because of such phenomena the temperature of the burnez-internals becomes too high and serious burner damage will occur. Further, there are problems with corrosion of the gas burner tips.
It is an object of-the..invention.to-provide a process for partial oxidation of a gaseous hydrocarbon-containing fuel wherein a good and rapid mixing or contacting of oxygen-containing gas (oxidiser), fuel and, optionally, moderator gas in the gasification zone is achieved beyond the exit of the burner and wherein burner-damage by corrosion, pre-ignition or flame-flash-back is suppressed.
The invention solves the above burner damage problem in that in the process of the invention the oxygen-containing gas applied as oxidiser and the gaseous hydrocarbon-containing fuel are supplied to the gasification zone through specific passages at specific velocities.
The invention therefore provides a process for the manufacture of synthesis gas by reacting oxygen-containing gas, applied as oxidiser, and gaseous hydrocarbon-containing fuel in a reaction zone of a substantially non-catalytic gas genera~ot comprising the steps of injecting the said fuel and the said oxidiser into the reaction zone through a multi-orifice ico-annular) burner comprising an arrangement of n separate passages or channels coaxial with the longitudinal axis of said burner, wherein n is an integer _> 2 (2, 3, 4, 5 ...), wherein the (n-1)th passage is the inner passage with respect to the nth passage, measured from the longitudinal axis of the said burner, and wherein the said gaseous hydrocarbon-containing fuel (optionally with a moderator gas) is passed through one or more of the passages, but at least through the nth passage, whereby at least one passage remains; the said oxidiser (optionally with a moderator gas) is passed through one or more of the remaining passages, but at least through the (n-1)th passage, and in such a manner that in any two adjacent passages in Which oxidiser is passed through the one passage, and gaseous hydrocarbon-containing fuel is passed through the other passage, the said oxidiser has a higher velocity than said hydrocarbon-containing fuel, and provided that when n is 4, then all four passages are used.
In this manner the oxygen-containing gas (oxidiser) entrains the gaseous hydrocarbon-containing fuel after which the partial oxidation takes place in the gasification zone, and the burner-internal blades that form the internal separation wall between the oxygen-containing gas (oxidiser) and the hydrocarbon-containing gas and which have a finite thickness, are cooled by the oxygen-containing gas (oxidiser) and the hydrocarbon-containing gas (in particular by connective cooling) to lower the flame temperature just behind the tips.
Behind the tip of the blade there is unavoidably at least a recirculation area in which both gaseous fuel and oxygen-containing gas, applied as oxidiser, are present.
If the hydrocarbon-containing gas would have the highest velocity, there will be oxygen-rich conditions at the burner-internal-tip by means of "entrainment" which will lead to high flame temperatures, high tip temperatures and serious loss of burner material.
If the oxygen-containing gas, applied as oxidiser, has the highest velocity, in the recirculation area there will be mainly oxygen-depleted conditions, which will lead to lower flame temperature. Thus, serious burner damage will not occur, which leads i.,;;~,,,;
', ;' ;', ,',' ' ~~v.
- 4 _ ~' 95554 to a long burner-lifetime.
Advantageously, for n 2 3, at least part (e.g. 20$) of the gaseous hydrocarbon-containing fuel is passed through the said nth passage and the remainder of the gaseous hydrocarbon-containing fuel is passed through one or more of the remaining passages. The ( velocity of the oxygen-containing gas, applied as oxidiser, is advantageously 20-150 m/s.
The velocity of the gaseous hydrocarbon-containing fuel is advantageously 0.2-0.8 times the velocity of the oxygen-containing gas, applied as oxidiser, in any two adjacent passages in which oxidiser is passed through the one passage, and gaseous hydrocarbon-containing fuel is-passed through the other passage.
In an advantageous embodiment pf the invention the respective velocities are measured or calculated at the outlet of-the said respective channels into the gasification zone. The velocity measurement or calculation can be carried out by those skilled in the art in any way suitable for the purpose and will therefore not be described in detail. -In another-advantageous embodiment of the invention-the moderator gas is steam and/or water and/or carbon dioxide and the oxidiser contains at least 90$ pure 02. In-still anothei advantageous embodiment of the invention the gasification process is carried out at a pressure of-.0_1-12 MPa abs.
Multi-orifice burners comprising arrangements of annular , concentric channels for supplying oxygen-containing gas (oxidiser), fuel and moderator gas to a gasification zone are known as such (vide e.9. EP-A-0,545,281 and DE-OS-2,935,754) and the mechanical structures thereof--will therefore not be described in detail.-Usually such burners comprise a number of slits at the burner outlet and hollow-wall members with internal cooling fluid (e. g.
water) passages. The passages may or may not be converging at the burner outlet. Instead of comprising internal cooling fluid passages, the burner may be provided with a suitable ceramic or refractory lining applied onto or suspended by a means closely adjacent to the outer surface of the burner (front) wall for W096103345 _.. __ _ _ PGTYEP95I02877 y.a :. ! .5 ~: ~ 195554 -5_ resisting the heat load during operation or heat-up/shut down situations of the burner.
y No fuel passage is reserved for a fuel other than gaseous hydrocarbon-containing fuel.
The invention will now be described in moze detail by reference to the following examples.
A number of examples are given in the Table. In this Table the following abbreviations are made:
Feed l:Natural Gas with the following typical composition CHq : 94.4$ by volume C2H6 . 3.0$
C3H8 . 0.5$
C4H10 : 0.2$
CSH12+: 0.2$
. C02 . 0.29 N2 . 1.5$
The supply temperature to the burner.of this feedstock is 150-2so ac.
Feed 2: Natural Gas with the following typical composition CH4 : 81.8$ by volume C2H6 . 2.7$
C3H8 . 0.4$
C4H10 : O.I$
CSH12+: 0.1$
_Cp2 . 0.9$
N2 : 14.0$
C02._is supplied as a moderator gas to the said natural gas in such a manner that the mass ratio of moderator gas C02 to Natural Gas is 0.6-0.8. The supply temperature to the burner of this feedstock is 280-320 °C~-_ oxidiser l: 99.5$ pure 02 with a temperature of 230-250 °C.
oxidiser 2: a mixture of a gas with 99.5$ pure 02 with 20-30$ (by mass) of moderator gas. This mixture has a temperature of 250-270 °C
and the moderator gas is steam at a temperature of 280-300 °C.
r.: 2 i 95554 ~,'- ~ ,~ ,~, ;. : .,;
A number of 9 examples has been presented. The following Table indicates the distributions of the respective fuels and oxidisers for these examples. The typical synthesis gas compositions are also given. The values of n as used in the description and claims are indicated and passage 1 is the first-or central passage. !
r ~(~'~r'~' t 2.1.95 ~ ~.4 _,_ Table With Examples Exam 1e number 1 2 g Value of n 7 6 6 'S Typical synthesis gas composition -3 -7 -3 CO [8 Vol, dr ]
CO [B Vol, dr ] 34-35 39-40 34-35 i H [8 Vol, dr ] 62-63 47-48 62-63 Reactor ressura [MPa]9-5 2-3 5-, Reactor temperature Ide CI 300-1400 250-1350 300-1400 Passa a 1 T a of feed 1 oxidiser oxidiser 1 as 1 Mass flow [k /s] 1-1.5 1.2-1.8 1-1.5 i Velocit [m/s] 30-45 80-120 50-75 Passa a 2 T a of oxidiser feed 2 feed 1 as 1 Mass flow jk Js) 2.6-4 0.9-0.6 1.1-1.6 i Velocit [m/s] BO-120 30-45 25-35 - Passa a 3 T a of feed 1 feed 2 oxidiser 1 as Mass flow [k /s] 2.1-3.1 2.1-3.1 2-3 Velocit [m/s] 30-45 80-120 50-75 Passa a 4 T a of oxidiser feed 2 feed 1 1 as 1 Mass flow [k /s] 2.7-4 0.6-0.9 1.8-2.7 Velocit [m/s] 80-120 30-45 25-35 Passa a S T a of feed 1 oxidiser oxidiser 1 as 1 .
Mass flow [k /s] 2.1-3.1 1.2-1.8 2-3 Velocit [m/s] 30-45 80-120 50-75 Passa a 6 T a of oxidiser feed 2 feed 1 as 1 f Mass flow [k /s] 3-4.5 0.76-1.1 1-1.5 Velocit [m/s] 80-120 30-45 20-30 ) Passa a 7 T a of feed 1 as Mass flow (k /s1 1-1.5 Velocit [m/s] 30-45 ~ic~=~t ~:~. ; ,_ -8_ Table With Examples (Continued) Exam 1e aumber 4 S 6 Value of n 5 4 3 Typical synthesis gas composition -10 -5 -5 CO [~ Vol, dr ]
CO [8 Vol, dr ] 36-37 32-33 32-33 H [fl Vol, dr ] 47-48 62-63 62-63 Reactor ressure [MPa]2-3 I-1.5 2-3 Reactor temperature [de C] 1200-1300 1300-1400 1300-1400 Passa a 1 T a of as feed 2 feed 1 feed 1 Mass flow [k /s] 1-1.5 - 2-3 0.7-1.1 Velocit [m/sj 40-60 80-120- 45-80 Passa a 2 T a of as oxidiser.2 feed 1 oxidiser 1 Mass flow (k /s] 1.6-2.4 0.6-0.9 1.7-2.6 Velocit [m/s] 95-140 30-45 100-150 Passa a 3 T a of as feed 2 oxidiser feed 1 Mass flow [k /s] 2-3 6.2-9.3 0.9-1.3 Velocit [m/s] 40-60 80-120 35-40 Passa a 4. T a of oxidiser feed 1 moderator as as 2 Mass flow (k /s] 1.6-2.4 1.3-2 0.6-0.9 Velocit [m/s] 70-100 25-35 55-80 Passa a 5 T a of as feed 2 Mass flow [k /s] 1-1.5 Velocit (m/s] 30-45 '~'~~Vr~~ i 4~ _ g _ ~~~~554 Table With Examples (Continued) Exam 1e number 7 8 g Value of n 3 3 2 3 Typical synthesis gas composition -5 -3 -5 CO [8 Vol, dr ]
CO [8 Vol, dr ] 32-33 34-35 32-33 H [6 Vol, dr ] 62-63 62-63 62-63 Reactor ressure [MPa]2-3 4-5 7-10 Reactor temperature [de C] 1300-1400 1300-1400 1300-1400 Passa a 1 T a of as oxidiser feed 1 oxidiser 2 Mass flow [k /s] 2.5-3.5 2-3 6-8 Velocit [m/s] 40-60 40-70 95-60 .
Passa a 2 T a of as oxidiser oxidiser feed 1 Mass flow [k /s] 1.7-2.6 4-6 4-5.6 Velocit [m/s] 100-150 80-120 25-35 Passa a 3 T a of as feed 1 feed 1 Mass flow [k /s] 2.5-3.7 1.3-2 Velocit [m/s] 30-45 30-45 It will.be appreciated by those skilled in the art that any slit width suitable for the purpose can be applied, dependent on the burner capacity.
Advantageously, the first or central passage has a diameter up to 70 mm, whereas the remaining concentric passages have slit widths in the range of 1-20 mm.
Various modifications of the present invention will become apparent to those skilled in the art from the foregoing description.
Such modifications are intended to fall within the scope of the appended claims.
Claims (14)
1. A process for the manufacture of synthesis gas by reacting an oxygen-containing gas, applied as oxidiser, and a gaseous hydrocarbon fuel in a reaction zone of a substantially non-catalytic gas generator comprising the steps of injecting the fuel and the oxidiser into the reaction zone through a multi-orifice (co-annular) burner comprising an arrangement of n separate passages or channels coaxial with the longitudinal axis of the burner, wherein n is an integer >= 2, wherein the (n-1)th passage is an inner passage with respect to the n th passage, measured from the longitudinal axis of the burner;
passing the gaseous hydrocarbon fuel, optionally with a first moderator gas, through one or more of the passages, but at least through the n th passage, whereby at least one passage remains; and passing the oxidiser, optionally with a second moderator gas, through one or more remaining passages, but at least through the (n-1)th passage, and in such a manner that in any two adjacent passages in which oxidiser is passed through the one passage, and gaseous hydrocarbon fuel is passed through the other passage, the oxidiser has a higher velocity than the hydrocarbon fuel, and provided that when n is 4, then all four passages are used.
passing the gaseous hydrocarbon fuel, optionally with a first moderator gas, through one or more of the passages, but at least through the n th passage, whereby at least one passage remains; and passing the oxidiser, optionally with a second moderator gas, through one or more remaining passages, but at least through the (n-1)th passage, and in such a manner that in any two adjacent passages in which oxidiser is passed through the one passage, and gaseous hydrocarbon fuel is passed through the other passage, the oxidiser has a higher velocity than the hydrocarbon fuel, and provided that when n is 4, then all four passages are used.
2. The process as claimed in claim 1, wherein the velocity of the gaseous hydrocarbon fuel is 0.2-0.8 times the velocity of the oxidiser in any two adjacent passages in which oxidiser is passed through the one passage, and gaseous hydrocarbon fuel is passed through the other passage.
3. The process as claimed in claim 1 or 2, wherein, for n >= 3, at least part of the gaseous hydrocarbon fuel is passed through the n th passage and the remainder of the gaseous hydrocarbon fuel is passed through one or more remaining passages.
4. The process as claimed in claim 3, wherein at least 20% of the gaseous hydrocarbon fuel is passed through the n th passage.
5. The process as claimed in any one of claims 1 to 4, wherein the velocity of the oxidiser is 20-150 m/s.
6. The process as claimed in any one of claims 1 to 5 carried out at a pressure of 0.1-12 MPa abs.
7. The process as claimed in any one of claims 1 to 6, wherein the gaseous hydrocarbon fuel is natural gas.
8. The process as claimed in any one of claims 1 to 7, wherein the oxidiser contains at least 90% pure oxygen.
9. The process as claimed in any one of claims 1 to 8, wherein the velocity of the oxidiser and the velocity of the gaseous hydrocarbon fuel are measured or calculated at outlets of the concentric passages or channels through which the oxidiser and hydrocarbon fuel are passed into the reaction zone.
10. The process as claimed in any one of claims 1 to 9, wherein the first moderator gas is steam, carbon dioxide or water or a combination thereof.
11. The process as claimed in any one of claims 1 to 10, wherein the second moderator gas is steam, carbon dioxide, water or a combination thereof.
12. The process as claimed in any one of claims 1 to 11, wherein a third moderator gas is passed through an (n+1)th passage.
13. The process as claimed in claim 12, wherein the third moderator gas is steam, carbon dioxide, water or a combination thereof.
14. The process as claimed in any one of claims 1 to 13, wherein no passage is reserved for a fuel other than gaseous hydrocarbon fuel.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP94202150.2 | 1994-07-22 | ||
| EP94202150 | 1994-07-22 | ||
| PCT/EP1995/002877 WO1996003345A1 (en) | 1994-07-22 | 1995-07-18 | A process for the manufacture of synthesis gas by partial oxidation of a gaseous hydrocarbon-containing fuel using a multi-orifice (co-annular) burner |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2195554A1 CA2195554A1 (en) | 1996-02-08 |
| CA2195554C true CA2195554C (en) | 2007-04-10 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002195554A Expired - Fee Related CA2195554C (en) | 1994-07-22 | 1995-07-18 | A process for the manufacture of synthesis gas by partial oxidation of a gaseous hydrocarbon-containing fuel using a multi-orifice (co-annular) burner |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA2195554C (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114231320B (en) * | 2021-11-29 | 2023-04-14 | 北京航化节能环保技术有限公司 | Coal gasification device capable of operating under variable load |
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1995
- 1995-07-18 CA CA002195554A patent/CA2195554C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CA2195554A1 (en) | 1996-02-08 |
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