AU605388B2

AU605388B2 - Partial combustion burner with spiral-flow cooled face

Info

Publication number: AU605388B2
Application number: AU26373/88A
Authority: AU
Inventors: Hendrikus Johannus Antonius Hasenack; Ian Poll
Original assignee: Shell Internationale Research Maatschappij BV
Current assignee: Shell Internationale Research Maatschappij BV
Priority date: 1988-02-17
Filing date: 1988-11-29
Publication date: 1991-01-10
Anticipated expiration: 2008-11-29
Also published as: CN1011617B; JPH028603A; CN1035172A; EP0328794B1; JP2627552B2; AU2637388A; EP0328794A1; DE3862757D1; CA1308306C

Description

S F Ref: 75073 FORM COMMONWEALTH OF AUSTRIN Afl) PATENTS ACT 1952 4 (p.

COMPLETE SPECIFICATION

(ORIGINAL)

FOR OFFICE USE: 44 Complete Specification Lodged: Accepted: 4t Published: Class Int Class dotj-je~jt ji stile !t1 IWths t L0 49 ni2a:e t.

9 Priori ty: Related Art: Name and Address of Applicant: Shell Internationale Research Maatschappij BV, Carel van Bylandtlaan 2596 HR The Hague THE NETHERLANDS Spruson Ferguso-n, Patent Attorneys Level 33 St Martins Tower, 31 Market Street Sydney, New South Wales, 2000, Australia Address for Service: Complete Specification for the Invention entitled: Partial Combustion Burner with Spiral-Flow Cooled Face The following statement is a full description of this invention, Including the best method of performing It known to me/us 5845/4 91-1- 1 T 8188 PARTIAL COMBUSTION BURNER WITH SPIRAL-FLOW COOLED FACE The invention relates to a burner for use in the partial combustion of carbonaceous fuels, and particularly for the partial combustion of finely divided solid fuel such as pulverized coal, in which the fuel is introduced together with an oxygen-containing gas into a reactor space operating under a pressure up to 100 bar for producing pressurized synthesis gas, fuel gas or reducing gas.

Partial combustion, also known as gasification, of a solid carbonaceous fuel is obtained by the reaction Sf the fuel with oxygen. The fuel contains as S• combustible components, mainly carbon and hydrogen, which react with the supplied oxygen and possibly 4. 4, with any steam and carbon dioxide as may be present to form carbon monoxide and hydrogen. At some temperatures it is also possible to form methane.

There are in principle two different processes for the partial combustion of solid fuel. In the first S process, solid fuel in particulate form is contacted with an oxygen-containing gas in the reactor in a fixed or fluidized bed at a temperature below about 1000 C.

A drawback of this method is that not all types of solid fuel can be partially combusted in this manner.

For example, high swelling coal is unsuitable since particles of such coal type easily sinter, resulting in risk of clogging of the reactor.

A more advantageous process passes the finely V divided fuel in a carrier gas such as nitrogen or synthesis gas into a reactor at relatively high velocity. In the reactor a flame is maintained in which the fuel reacts with oxygen-containing gas at

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r* 9 9 '9 *1 9 9. 9 9e 9, 9 .9 *O 94 99 *4 4i .4 4* 9 1 2 temperatures above 1000 C. The carbonaceous fuel is usually passed into the reactor via a burner, and the oxygen-containing gas is also passed via the burner into the reactor. In some processes a moderator gas such as steam or carbon dioxide is also passed via the burner to the reactor; such a moderator gas is often advantageous for reducing or preventing premature contact of the oxygen with the reactor gas, which might result in undesirable complete conversion of the reactor gas.

The present burner is well suited to introduce the reactants in any desired manner, vertically or horizontally, into the reaction zone of a conventional, refractory lined partial oxidation gas generator, and is particularly suited for use in solid fuel gasification apparatus having a plurality of burners for the reactants positioned on substantially opposite sides of the combustion zone, whereby the reactants are introduced horizontally and the burner jets impinge on each other to facilitate the partial oxidation process and to minimize erosion of the refractory wall.

Since flame temperatures may reach 2000°C or more, a primary concern of such burners is to prevent damage to the burner front, also referred to as the burner face, caused by the high heat flux during the gasification process. To protect the burner front from overheating, it has been suggested to provide a refractory lining applied to the outer surface of the burner front wall and/or provide a a hollow wall member with internal cooling passages through which cooling fluid is circulated at a rapid rate.

It is therefore an object of the present invention to provide a burner wherein the cooling fluid is caused to flow in a particular manner to assure even cooling of the burner front face so as to minimize thermal, 9911 F 3 stresses which could cause deterioration and even failure of the burner during prolonged operation.

The invention therefore provides a burner for the partial combustion of finely divided solid carbonaceous fuel with an oxygen containing gas In a combustion zone, characterized by: a central channel and outlet for supplying fuel to the combustion zone; at least one first substantially annular channel disposed coaxially with said cent;'al channel and having an outlet to supply an oxygen-containing gas flow to the combustion zone; a front face disposed at a discharge end of said burner and normal to a longitudinal axis thereof, said front face having a central aperture through which at least said fuel and oxygen-containing gas flow to the combustion zone; said front face comprising a hollow wall member operatively connected to: a supply conduit disposed to supply fluid coolant to the proximate first end of a passageway in said hollow wall member; a return conduit disposed to pass fluid coolant proximately from the final end oi' said passageway; and Including spiral flow means defining said passageway disposed within said hollow wall member to cause fluid coolant entering said hollow wall member from said supply conduit to flow In a spiral direction about the longitudinal axis of the burner.

to' Advantageously a second substantially annular channel is disposed coaxially with said first annular channel and having an outlet to supply a second gas flow to the combustion zone, In this manner the Invention provides a burner that Is capable of operation for extended periods of -ti A 4/ KXH 1019y

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time without subjecting the front face and other burner components to excessive stress.

The invention will now be described in more detail, by way of example, with reference to the accompanying drawings, wherein: FIG. 1 is a longitudinal section of the front part of a burner according to the invention; FIG. 2 shows a cross-section along the line 11-11 of FIG. 1; FIG. 3 Is a longitudinal section of the front part of another burner according to the invention; and FIG. 4 shows a cross-section along the line 111-111 of FIG. 3.

It should be noted that identical elements shown in the drawings have been indicated with the same reference numeral.

Referring to FIGS. I and 21 a burner, generally indicated with the reference numeral 10, for the partial combustion of a carbonaceous fuel, such as pulverized coal comprises a central channel 12 disposed along a longitudinal axis 14, and having a discharge outlet 16 for supplying a finely divided solid fuel (arrow A) in a carrier gas, nitrogen, carbon dioxide or synthesis gas, to a combustion zone.

Concentrically arranged around the central channel 12 is a first substantially annular channel 18 for an oxidant gas (arrow B) having a free end 20 forming an outlet for said oxidant gas flow into the combustion zone. Advantageously, the outlet 20 is disposed at an angle of from about 15 to about 60 degrees with respect to the longitudinal axis 14, so that the issuing stream of oxygen-containing gas will intersect and mix with the stream of solid fuel issuing from outlet 16 into the downstream combustion zone. The oxidant gas will be oxygen-containing gas, or optionally a mixture of

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5 9 .4 *P 4 Ii I 9, h41 9 4t 4 N 4 oxygen-containing gas with a moderator gas such as, steam or carbon dioxide. Conventional separators are used for radially spacing the channels from each other, for example alignment pins, fins, centering vanes, spacers and other conventional means are used to symmetrically space the channels with respect to each other and to hold same in stable alignment with minimal obstruction to the free flow of the reactant streams.

The burner 10 further comprises a cylindrical hollow wall member 26 having an enlarged end part forming a front face 28 which is normal to the longitudinal axis 14 of the burner. The hollow wall member is interiorly provided with spiral flow means 29, which may be somewhat pervious to fluids, but advantageously is a fluid impervious barrier forming a spiral channel 30, said channel having one end operatively connected to supply conduit 34 for supplying fluid coolant (arrow C) to said spiral channel and having the other end of said spiral channel operatively connected to return conduit 32 to pass fluid coolant from said channel 30 (arrow The supply conduit may be operatively connected to either end of the spiral channel, and the return conduit to the other end, as desired. However, advantageously the supply conduit provides the fluid coolant, particularly a liquid coolant such as tempered water to the outside end of spiral channel It is an advantage of the present invention that it permits convective and radiant heat transfer from the combustion downstream of the burner face while avoiding, substantially or altogether, boiling of the coolant liquid within the hollow wall member. The use of high velocity coolant through the spiral channel assures even, low metal temperature in the burner face thereby enabling long life of the burner.

444n 9 4 *4 4* i d .111 A 6 When water is used as coolant, it is supplied to the hollow wall member at a flow rate sufficiently high that at maximum heat output of the burner the water entering the return conduit will have increased no more than about 5°C and more in particular less than about 3°

C

It is found advantageous to employ as coolant tempered water having a temperature in the range below about 210 0

C.

During operation of the above described burner for the gasification of carbonaceous fuel, e.g., pulverized coal by means of oxygen-containing gas, said coal suspended in a carrier fluid, such as, e.g., nitrogen, synthesis gas or carbon dioxide, is passed 1 through the central channel 12 to outlet 16 for introducing the coal into the combustion zone of a ,i reactor arranged downstream of the burner.

Simultaneously, oxygen-containing gas is passed through annular channel 18 to outlet 20 so that the coal and oxygen-containing gas reactants will be intensively mixed in the reactor space. The mixing of the reactants can be further promoted by a swirling motion imparted to one or both streams by a swirl body of baffles (not shown) in the appropriate channel. To promote stable outflow of coal the cross sectional area 'available for the coal flow should be kept constant over at least part of central channel 12 of the burner near the outlet.

During operation of the burner for the gasification of pulverized fuel, a temperature moderating gas such as steam, carbon dioxide or nitrogen also may be introduced into the feed line of annular channel so that a mixture of oxygen-containing gas and moderating gas, is conveyed through annular channel 18 to outlet 20 to control the temperature and to limit the amount of oxygen as needed. The rate of 7 flow for each of the streams of pulverized fuel, and oxygen-containing gas optionally mixed with temperature moderator gas is controlled by a flow control valve (not shown) in each feedline upstream of the burner.

The burner firing rate, turnup or turndown of the burner, is effected by changing the flow rate for each of the streams while maintaining a substantially constant ratio of atomic oxygen to carbon in the solid feed. Generally an oxygen demand of 0.9 to 1 ton per ton of moisture and ash-free coal is fairly typical of hard coals; for low rank coals 0.7 tons oxygen per ton is more representative.

Referring now to Figs. 3 and 4 a burner is shown III wherein arranged concentrically around said first annular channel 18 is a second substantially annular channel 22 for a second gas, which may be oxygen-containing gas, a modor'tor gas such as, e.g., steam or carbon dioxide, or a mixture or oxygen-containing gas and moderator gas, and having free end 24 forming an outlet for a second gas flow into the combustion zone. Said outlet 24 will generally be disposed at a similar angle with respect to the longitudinal axis 14, but advantageously will be more divergent, less acute when said second annular channel will be used to supply moderating or shi2lding gas to the combustion zone. The ratio of the cross-sectional area for the second annular channel divided by thle cross-sectional area for the first annular channel is in the range from about 0.5 to 2, such as 0.75 to During operation of this burner for the gasification of pulverized fuel a second gas which may be oxygen-containing gas, a temperature moderating gas such as steam, carbon dioxide or nitrogen, or a mixture of oxygen-containing gas and moderating gas, is ^1 t-: 8- 11 t it i I I I IF it I

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I. I: I. F 14 I it ft II IF I I II 4 1 II F I I conveyed through annular channel 22 to outlet 24 to supply additional oxygen as needed, and when said second gas flow contains substantial amounts of moderator gas, forms a shield around the jets issuing coal and oxygen. The shield of moderator gas may be advantageous for preventing premature contact of oxygen W.11th the reactor gas, which might result in undesirable complete conversion of the reactor gas. It is preferred to operate by supplying oxygen-containing gas through both channels, at a mean velocity in the range from about 35 to about 100 meters/second, supplying said gas through said first (centermost) annular channel outlet at a somewhat lower velocity than the velocity of gas supplied to the combustion zone through said second annular channel outlet.

The rate of flow for each of the streams of the pulverized fuel, the oxygen-containing gas and of the seoond gas Is controlled by a flow control valve in each feedline to the burner. The burner firing rate, turnup or turndown of the burner, is effected by changing the flow rate for each of the streams while maintaining a substantially conctnt ratio of atomic oxygen to carbon in the solid feed. Generally an oxygen damand of 0.9 to 1 ton per toii of moisture and ash-free coal is fairly typical of hard coals; for low rank~ coals 0.7 tons oxygen per ton is more represantative.

It is an advantage of the instant burner in addition to its durability that it has a channel for admitting a second gas to the combustion zone that permits great flexibility in supplying the reactants under a wide variety of operational requirements.

The burner will ordinarily be fabricated of high temparature resistant materials, particularly high temperature resistaht metalo and alloys and be fabricated by techniques of welding and/or brazing 9- *1 I~ 4 4 ii 44 4 *44 44 ap 4 4 4 I 4* II 4 44 4 I .4 ft 4 4 4 *4 4 4. *4 *40* conventionally employed with such matezials. For high duty operations the c.hannels and outlets for oxygen-containing gas, which are usually made of metal, may be internally coated with an oxidic coating, such as ZrO 2 or a ceramiic, enabling the application of high oxygen-containing gas velocities without the risk of metal combustion by the oxygen.

The term solid carbonaceous fuel as used herein is intended to include various materials and mixtures thereof from the group of coal, coke fro~m coal, coal.

liquefaction residues, petroleum coke, soot and particulate solids derived from oi, shale, tar sands and pitch. The coal may be of any type, including lignite, sub-bituminous, bituminous and anthracite.

The solid carbonaceous fuels are advantageously ground to a particle size so that at least about 90% by weight of the material is less than 90 microns and moisture content is less than about five per cent weight.

The term l"oxy'gon-containing gas" as used herein is intended to refer to gas containing free oxygen, i.e., uncombined oxygen, and to Include air, oxygon-onriched air, greater than 21 mole oxygen, and also substantially pure oxygen, Lif greater than about mole k oxygen, with the remainder comprising gases normally found in air~ such as nitrogen and the rare gases, Various modifications of the invention will, become apparent to those skilled in the art from the foregoing description and accompanying drawings. such modifications are intended to fall. within the scope of the appended claims.

Claims

1. A burner for the partial combustion of finely divided solid carbonaceous fuel with an oxygen containing gas In a combustion zone, characterized by: a central channel and outlet for supplying fuel to the combustion zone; at least one first substantially annular channel disposed coaxially with said central channel and having an outlet to supply an oxygen-containing gas flow to the combustion zone; a front face disposed at a discharge end of said burner and normal to a longitudinal axis thereof, said front face having a central aperture through which at least said fuel and oxygen-contalning gas flow to the combustion zone; said front face comprising a hollow wall member operatively connected to: a supply conduit disposed to supply fluid coolant to the proximate first end of a passageway in said hollow wall member; a return conduit disposed to pass fluid coolant proximately from the final end of said passageway; and Including spiral flow means defining said passageway disposed within said hollow wall member to cause fluid coolant entering said hollow wall member from said supply conduit to flow in a spiral direction about the longitudinal axis of the burner. i

2. The burner as claimed In claim 1, characterized by a second substantially annular channel disposed coaxially with said first annular channel and having an outlet to supply a second gas flow to the combustion zone, and wherein said second gas flows to the i UX***tt y 11 combustion zone through the central aperture of said front face.

3. The burner as claimed in claims 1 or 2, characterized in that said spiral flow means comprises a continuous impervious barrier forming a spiral channel within said hollow wall member.

4. The burner as claimed in claims 1 or 2, characterized in that said hollow wall member, said final end of the passageway for cooling fluid is disposed adjacent to said central aperture. The burner as claimed in claim 2, characterized in that said first and second annular channels are each RA separately connected to oxygen-containing gas sources which are independently controllable as to pressure and So 4,low rate. S' 6, A burner for the partial combustion of finely divided solid carbonaceous fuel with an oxygen containing gas In a combustion zone :S substantially as hereinbefore described with reference to 4 the accompanying drawings, Sa, 7. Synthesis gas, fuel gas or reducinU gas produced In a burner as claimed in any one of claims I to 6. DATED this FOURTEENTH day of NOVEMBER 1988 Shell Internationale Research Maatschapplj B.V. S*1 PaEtnt Attorn.ys for the Applicant SPRUSON FERGUSON *i T4/T8188 I I I K 1 m