CN1439044A - Feed nozzle for gasification reactor for halogenated materials - Google Patents
Feed nozzle for gasification reactor for halogenated materials Download PDFInfo
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- CN1439044A CN1439044A CN 01808843 CN01808843A CN1439044A CN 1439044 A CN1439044 A CN 1439044A CN 01808843 CN01808843 CN 01808843 CN 01808843 A CN01808843 A CN 01808843A CN 1439044 A CN1439044 A CN 1439044A
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- nozzle
- passage
- gas
- halogenated materials
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23D—BURNERS
- F23D11/00—Burners using a direct spraying action of liquid droplets or vaporised liquid into the combustion space
- F23D11/10—Burners using a direct spraying action of liquid droplets or vaporised liquid into the combustion space the spraying being induced by a gaseous medium, e.g. water vapour
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- 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
- C10J3/48—Apparatus; Plants
- C10J3/50—Fuel charging devices
- C10J3/506—Fuel charging devices for entrained flow gasifiers
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2200/00—Details of gasification apparatus
- C10J2200/15—Details of feeding means
- C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
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- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23D—BURNERS
- F23D2900/00—Special features of, or arrangements for burners using fluid fuels or solid fuels suspended in a carrier gas
- F23D2900/00006—Liquid fuel burners using pure oxygen or O2-enriched air as oxidant
Abstract
Method and apparatus for feeding halogenated material to a gasification reactor including supplying a gaseous source of oxygen at supersonic velocity and discharging a liquid halogenated material from at leat one discharge port radially peripheral to discharging oxygen source gas such that the oxygen gas atomizes the liquid halogenated material into the gasification reactor.
Description
The present invention relates to the feed nozzle of gasifying reactor, or rather, relate to the feed nozzle of the gasifying reactor of halogenated materials, particularly halogenated organic matters and chlorinatedorganic (RCl), be called burner sometimes.
Related invention comprises the patent application formerly of producing the method and apparatus of one or more useful products from the halogenated materials of low value, and this patent application is PCT International Application PCT/US/98/26298 that on July 1st, 1999 is disclosed, international publication number is WO 99/32937.This PCT application discloses raw material, the particularly by product that will be made up of halogenated materials basically by the partial oxidation reforming step in elementary gasifying reactor and secondary discrete type " suction " reactor and the method and apparatus that changes into one or more " high value products " from the useless hydrochloric ether that various chemical preparation processes produce.
In general, the gasifying reactor of halogenated materials preferably includes the refractory liner cylindrical vessel that at one end is connected with mixing nozzle.With halogenated materials, the normally mixture of RCl or all kinds of material, oxygen and most probable steam, and optionally additional gas fuel, water/hydrogen halide steam and CO
2The process feed nozzle joins in the gasifying reactor together and atomizes, and generates the gasiform partial oxidation products.A typical cover operational condition be included in about 30 ℃ and 7 crust (100psig) standard pressures down the flow of liquid state (optionally carry out preheating or anticipate) halogenated hydrocarbon charging near 170 liters/minute (45 gallon per minute).Under 120 ℃ and 14 crust (200psig) pressure oxygen with about 450 kilograms (10,000lbs)/hour supply.Steam and oxygen with near 450kg (10,000lbs)/hour speed provide, and saturated under (150psig) pressure at 10 crust.The pressure of reactor is 5 crust (75psig), and temperature of reactor is preferably between 1300 ℃ and 1500 ℃.
The suitable dispersion that joins the liquid halo raw material in partial oxidation (gasification) reactor is a crucial step for the successful operation of gasification.The Action Target of dispersing nozzle (being called burner sometimes) comprises the raw material to wide region, and reactor can carry out the difficult target of stable operation, and halogenated materials almost completely reacts simultaneously, and the raw material of partial reaction is minimized.General requirements for the reactor feed nozzle under harsh day by day gasification environment has proposed difficult performance constraint really.For relatively, even also propose or provide than at this more benign environment of considering, known that the design of nozzle and performance are restrictive factors for the reliability of reactor in the association area of gasification.
For example, when comparing with coal gasification course or even when comparing with the gasification of the non-halogenated materials of other carbon containing, the RCl gasification exists unique problem.On the one hand, halogenated materials, for example hydrogenchloride has very strong corrodibility.Secondly, liquid, for example the feed stream of the gasifying reactor of liquid RCl is compared with the gasification of many routines and is had different attributes.For the optimum operation of halogenated materials gasifying reactor, must supply the many different feed stream of halogenated materials.Need have multiple feed conduit, if charging simultaneously then needs the structure of conduit can avoid the unwanted each other reaction of multiple feed logistics in the nozzle from the multichannel source of halogenated materials.
For the purpose of gasifying reactor, the feed nozzle of prior art is tending towards utilizing internal mix in nozzle, thereby helps to guarantee effective decomposition of liquid stream.For example, inside mix nozzle is known for fuel oil atomization, and believes that this application has obtained the highest operation efficiency.But internal mix is not a preferable methods under present environment.Halogenated materials and oxygen carry out internal mix and enter nozzle and increased about security and active worry.Internal mix in the nozzle pollutes the nozzle inboard after shut-down, and the charging tar when stopping work may be coated in the inside of nozzle.This pollutent may cause oxidizing reaction in nozzle.Therefore, an object of the present invention is security and reactive aspect obtain better effective external mix nozzle.These high pressure drops of considering the complicacy that increases than the multiport design and/or lower nebulization efficiency and/or oxygen are more important.But, should be realized that the graceful simple required advantage of mixing nozzle always of design simultaneously, thereby can have higher vapourizing furnace reliability.This also with the design simplicity as an advantage, but its be subordinated to reality the operational constraints condition.
As mentioned above, feed nozzle or burner are the significant components of the globality of gasifying reactor.Discharge spray from burner is to carry out the blended momentum source in the vapourizing furnace, and main burning furnace must enter liquid fuel atomization this mixing jetting stream.Typical atomization target is that 99% liquid volume is atomized into 500 microns or littler drop size.Enough liquid surface area are provided like this, thereby can have carried out the rapid evaporation of fuel.Two kinds of mechanism work in this atomization process.In preferred embodiments, inject liquid, the coarse atomization process of the liquid jet that the pressure drop by these holes begins to disperse by the hole that is positioned at the circular permutation at center around the maincenter oxygen discharging.Therefore, spray orifice and liquid jet preferably intersect in the place ahead in burner front, more clearly say so to intersect with oxygen discharge injection stream along the axle of oxygen discharging.In this mode, oxygen is discharged injection stream and is provided main energy for microatomization.The static pressure of oxygen converts kinetic energy to by burner nozzle.Nozzle is preferably near sound wave, or more preferably ultrasonic nozzle, therefore can obtain top speed.The difference of speed is the atomizing energy that liquid jet is resolved into trickle discrete droplets between gas and the liquid.In preferred operating method, the moderator logistics of steam can be mixed with the oxygen upstream of burner.The oxygen that enters vapourizing furnace preferably is preheated to 120 ℃, thereby therefore the temperature fall of compensation oxygen when expanding by nozzle increased nebulization efficiency.
Another aspect of the present invention is the expansion energy that utilizes the oxygen source gas of leaving through nozzle, thereby externally decomposes and the logistics of the liquid feeding of atomizing collision fine.The favourable use of gas expansion energy is mixed into feed nozzle with the collision liquid stream of oxygen source gas and outside, and outside liquid is atomised in the nozzle fully.This design utilizes to such an extent that effective merit of self-expanding oxidizing gas encourages, atomizes and injecting LPG in liquefied condition enters chamber of the reactor, and the gas passage that wherein described expansion oxidizing gas is dwindled, preferably forms by the inwardly projecting orifice structure is then expanded.Oxygen source gas can be oxygen, steam and/or other gas.Usually this gas is purity oxygen.The velocity of discharge maximization of (converging then diverging) design of preferably contracting-expand of oxygen channel with gas.One aspect of the present invention is structure and operates the oxygen channel that contracts-expand, thereby dwindling the acoustic wave flow that the part end obtains oxygen source gas.Obtain ultrasonic flow at subsequently passage expansion then.(still, can optionally use the nozzle that can only dwindle, if particularly oxygen source gas is enough to contracting-expanding because of pressure ratio can not accelerate in the designs of nozzles when operating with acoustic wave flow.Usually, though can use the designs of nozzles that to dwindle, should be taken into account the efficient that it is littler.)
Flame temperature above 3000 ℃ can reach the mixing of oxygen source gas and halogenated materials charging.This temperature (although realizing at the downstream end a little of nozzle) is quantity of radiant energy backward, thus the downstream part of heated nozzle, and may shorten life-span of nozzle.Therefore, the cooling of nozzle end part or the downstream end of nozzle partly are another aspects of the design.Cool off by several methods, this method comprises carries out the loop that steam film cools off and/or provide at the housing parts of nozzle self heat-eliminating medium (for example water) to the outside of nozzle body.Water cooling chuck (though more complicated than the steam film cooling) is for feed nozzle industry provides the other design that has been confirmed, and is also that it is open as other cooling system at this.The simpler Machine Manufacturing Technology of steam film cooling jacket utilization provides advantage for the control metallic surface temperature.
Another aspect of the present invention can provide such as steam or CO
2Or effective " rare gas element " of HCl steam and so on, thereby produce " rare gas element " curtain at nozzle end, so that further improve the radiation of carrying out from the thermal reaction area in nozzle downstream backward.The present invention provides design for from the discharging of thermal reactor environment separation oxidizing gas the ring-type of effective " rare gas element " being sprayed, thereby helps avoid the influence that the interior material of nozzle is subjected to reaction heat." rare gas element " curtain that provides part to comprise oxygen discharging can be removed the potential burning in nozzle arrangements, make the position of top temperature move and away from the downstream end face of nozzle.This protection has reduced the potential thermal stresses of nozzle end material and has prolonged the life-span of nozzle.Therefore, for fear of (producing the condition of top temperature), preferably " moderator " or its part are ejected in the vapourizing furnace with the form that is enclosed in oxygen/fuel injection stream annular membrane on every side the positive directly product in the thermal reaction chamber being incorporated in the proximate purity oxygen of burner.This 'inertia' layer is tending towards removing the thermooxidizing band from burner face, therefore, has reduced the heat outflow and reduced the temperature that reaches on burner face.CO
2Can absorb ir radiation because of it but preferred effectively rare gas element with steam.
For can with different liquid feeding logistics respectively and side by side (if desired) join in the reaction chamber, another aspect of the present invention's design provides the fluid conduits that is used to distribute or separate halogenated materials.
The present invention includes with the gasifying reactor of halogenated materials carry out in conjunction with and be suitable for being connected thereon used feed nozzle.In a kind of embodiment preferred, nozzle provides the expansion first channel that contracts for the gas source of oxygen.This first channel ends at outlet orifice at the downstream end of nozzle.Though first channel can be made up of many littler passages that constitute, and considers single passage in preferred embodiments.
The liquid feeding logistics that is designed to halogenated materials of nozzle provides at least one second passage, and described second passage ends at least one relief outlet at the downstream end of nozzle.In some cases, the embodiment preferred plan provides a plurality of second passages, also reacts simultaneously so that add different halogenated materials.These halogenated materials can advantageously separate before entering reaction chamber.
Fluid flow is carried out in one or more second passages and liquid halogenated materials source.The relief outlet of one or more second passages be preferably designed to radially be positioned at the first channel outlet orifice around.
The 3rd effective " rare gas element " passage optionally is provided.This rare gas element most preferably is that steam or major portion are steam.The relief outlet that the third channel of this rare gas element (can be one or more littler composition passages) is preferably designed to adjacent second passage discharges.
The passage of rare gas element, oxygen source gas and halogenated materials and the appropriate sources of material are carried out fluid flow.Supply system provides suitable temperature and pressure control.
The downstream end that the steam that is utilized in " rare gas element " passage is preferably nozzle provides film cooling and " rare gas element " curtain, and it can avoid the nozzle end surface to be subjected to the influence of the maximum heat of gasifying reactor in the initial stage mixing zone.This steam also can be used as the reactant that oxygen and hydrogen source are provided.Guiding and/or pilot jet passage are provided in some embodiments.The selectivity design that can only dwindle is also disclosed simultaneously.
The present invention includes the method that the liquid halogenated materials is fed to gasifying reactor.This method comprises that gas source with oxygen is to be fed to the spray orifice that enters the feed nozzle in the gasifying reactor near sound wave or preferred hyperacoustic speed.Halogenated materials is discharged from the oxygen source gas relief outlet on every side that at least one radially is positioned at discharge, so that oxygen source gas can be supplied with the halogenated materials energy and in the downstream on feed nozzle surface its atomizing be entered the gasifying reactor chamber at least.This method is included as " rare gas element " curtain that nozzle surface provides water cooling and/or film cooling and the discharge end of adjacent nozzles is provided, thereby helps avoid the limit heat that nozzle surface is subjected to oxidizing reaction.Starting method also is provided in addition, and this method is utilized the feed gas passage and the oxygen source gas of small volume when slowly increasing oxygen velocity.
When considering the following detailed description of preferred embodiment in conjunction with following accompanying drawing, the present invention may be better understood, wherein:
Fig. 1 is the illustrative sectional view of the passage that contracts-expand of expression oxygen source gas; It also represents the circular permutation of the loop exit end of centre pilot nozzle and halogenated materials; It also illustrates the passage that is used for rare gas element cooling or steam cooling; The source of feed stream and the relief outlet of nozzle have also been expressed.
Fig. 2 and Fig. 1 are similar, and just the downstream end of the chuck of rare gas element cooling logistics has different configurations.
The nozzle that does not have the centre pilot nozzle in Fig. 3 presentation graphs 2.
Fig. 4 and Fig. 2 are similar, but have the independent feed-pipe of halogenated materials.
The another embodiment of Fig. 5 presentation graphs 4, it has sectional or independent feed-pipe for various halogenated materials.
Fig. 6 explanation has the nozzle in heat-eliminating medium loop.
Fig. 7 and 8 illustrates in greater detail gasification reaction process and gasification heater stage.
The nozzle that Fig. 9 explanation can only be dwindled, this nozzle can be suitable for any configuration among Fig. 1-6.
Fig. 7 and 8 with the form of flow sheet represented halogenated materials gasification reaction system and be suitable for the preferred embodiment of the present invention operation.Fig. 7 and 8 and be that the present invention lays the first stone at first are discussed.
The feedstock conversion that the gasification reaction process GPR of Fig. 7 will be made up of halogenated materials basically becomes one or more useful products.As shown in Figure 7, these products can be the forms of useful or vendible acid product 50 and/or product synthetic gas 54.(in addition, can be used as raw material in different purposes or vendible product synthetic from the reaction product (comprising identical hydrogenchloride, carbon monoxide and hydrogen component) of the partial oxidation reforming step of this process, it is not expressed in Fig. 7.)
As shown in Figure 7, special now preparation with reference to acid product 50 and/or product synthetic gas 54, this process comprises step: the vapourizing furnace of under partial oxidation reforming reactor zone or reduced pressure, operating 200 (the partial oxidation reforming reactor by one or more serial or parallel connections is formed (as shown in Figure 8)) supply charging 56, source of oxygen 58 and the hydrogeneous co-fed (not shown) of complementarity of moderator logistics (not shown) and required the best optionally, so that all basically halogenated materials change into corresponding halocarbon in the charging.
This process comprises step (describing by the preferred embodiment among Fig. 7): reclaim the reacting product stream of mainly being made up of one or more hydrogen halide, water, carbon monoxide and hydrogen 60 from reactor, this product stream contains unconverted halogenated materials hardly, removes stage 300, particle recovery stage 350, resorber stage 400, aqueous acids at quenching and particulate then and removes the stage 450 and separate with the synthetic gas precision work stage 700 and reclaim useful products.The useful products that reclaims from reaction product can comprise one or both available or vendible hydracid product and product synthetic gas.
Fig. 8 understands the operation of the preferred embodiment in vapourizing furnace stage 200 in more detail, and the Oxygen Flow 290 that its expression will the most suitably be heated by the oxygen preheat device E-290 of vapour stream 235 runnings is fed to main burner BL-200 as logistics 291.Simultaneously vapour stream 298 is joined in the main burner, it is preferably from the RCl feed stream 144 of preheater E-140 and fuel gas logistics 296 with from the cyclic steam stream 530 of upstream water distilling apparatus T-510.The nitrogen gas stream 295 of supply is carried out nitrogen purge with elementary vapourizing furnace R-200.In preferred embodiments, gasifying furnace device is represented with elementary vapourizing furnace R-200 and secondary vapourizing furnace R-210.
Method and apparatus of the present invention relates in particular to the feed nozzle BL-200 of gasifying reactor R-200.This designs of nozzles is useful for the atomizing of various halogenated materials chargings, and they is changed into the more product of high value in reaction process.Can be considered to use by this nozzle by the charging (for example, having chlorinated hydrocarbons chlorinated fluorocarbon and/or hydrochlorinate fluorocarbon) that the mixture of different halogenated materials is formed, it is to comprise liquid and solid charging.Preferred this nozzle material-feeding is made up of liquid basically or fully.More preferably this charging is substantially free of ash content and slag making, and this charging comprises less than 5% ash content and other inorganic substance, more preferably comprises 1% or this class material still less.
Gasifying reactor R-200 and R-210 preferably (preferably are selected from the form of the oxygen-containing gas of oxygen, air, oxygen-rich air and carbonic acid gas in source of oxygen with one or more under reduced pressure, but more preferably be oxygen basically) and the hydrogeneous co-fed existence that replenishes of selectivity under operate, this hydrogeneous co-fed can be in the reaction product that derives from partial oxidation reforming reactor zone with charging in all basically chlorine change into hydrogenchloride.Steam adds as temperature moderator and extra hydrogen source in the reformer of routine is implemented, and steam should be considered other reactant of being included as selectivity.
The typical operation of combustors parameter of the design's nozzle is:
1. liquid fuel pressure drop: be 10 crust (150psi) under 140 liters/minute (37gpm).
For typical liquid orifice, square being directly proportional of pressure drop and flow.Fuel may stop up or aging (the low pressure reduction) of coking (High Pressure Difference) or nozzle end in the deviation of this relational expression explanation nozzle.
2. oxygen pressure drop: different fully with pressure drop by the ultrasonic nozzle that pressure ratio forms.Pressure ratio is the ratio of absolute pressure: P
U/ P
RThe standard operation ratio of oxygen 450kg/hr (10, be 2.75 000lb/hr).This is upstream absolute pressure (P
U) and vapourizing furnace chamber absolute pressure (R
R) ratio.
3. oxygen temperature: the oxygen temperature of burner should maintain 120 ℃.Because whole burner has higher pressure ratio, the oxygen outlet temperature is near 25 ℃ as a result.Lower temperature causes littler speed, lower nebulization efficiency and the longer evaporation time of burner.
4. moderator pressure drop: for this low pressure drop gas flow, pressure drop in fact with square being directly proportional of flow.Deviation shows the aging of the annular chamber that contains moderator.
According to top discussion, the feed nozzle of this operation (comprise this charging is delivered to this rigorous environment) is vital device significantly.Fig. 1 represents the preferred embodiment of feed nozzle of the present invention with sectional view.Expressed gasifying reactor wall part R around nozzle N.Terminal DSE is expressed as being positioned at the interior region GR that is drained into gasifying reactor with downstream nozzle.The expression of DP end is by the relief outlet of the radial array that is used for the halogenated materials charging of passage HMP transmission.Oxygen source gas flows into the outlet orifice DO of the terminal DSE of discharge that is positioned at feed nozzle N by passage OP from source of oxygen 10 (utilizing the currently known methods of this area).Fig. 1 represents that also effectively " rare gas element ", preferred steam flow into the rare gas element passage IGP that nozzle N forms from inert gas source 12.Rare gas element passage IGP is partly formed by the chuck J1 of nozzle N.Chuck J1 preferably represents with the form that contains outlet V at outer wall.Complementarity fuel gas such as methane the fuel gas channel FGP that 13 inflows also partly form by chuck J2 by nozzle N from the source.
Passage PP with one or more relief outlet PDP forms in directional nozzle PN, and this directional nozzle PN is positioned at the centre of oxygen source gas passage OP.Directional nozzle passage PP is connected with the source 11 of halogenated materials with halogenated materials passage HMP.The multichannel source of source 11 yes halogenated materials, and the halogenated materials in the multichannel source can be identical or different.The complementarity fuel gas 13 is fed to passage PP from originating.Passage PP is mainly the halogenated materials charging is delivered to the passage that one or more atomizing port PDP provide small cross section to amass.In the starting process of nozzle, the halogenated materials charging all is fed to nozzle with relative slow flow velocity with oxygen.For throughput provides the passage PP of smaller size smaller or sectional area feed material is atomized better under the lower overall flow rate at these initial stages.
Fig. 2 is different from Fig. 1, because part forms the downstream end DSE that the chuck J1 of rare gas element passage IGP is not centered around nozzle N.Chuck J1 helps to form " rare gas element " curtain of generation.
More fully describe according to following, Fig. 3 is different from Fig. 1 and 2, and it shows that embodiment preferred does not need in conjunction with the directional nozzle that forms guide channel PP, although this passage PP also can be used as the other or extra liquid halogenated materials passage that passes through nozzle center.
Fig. 4 is different from Fig. 1-3, because Fig. 4 specifically represents and the sectional that is used for halogenated materials or independent passage are provided, shown in passage HMP1 and passage HMP2 among Fig. 4.This sectional or independent passage provide passage for the inhomogeneity halogenated materials, and the relief outlet at nozzle mixes halogenated materials in gasifying reactor simultaneously.In addition, also cyclic halogenated materials passage can be cut apart and form isolating passage.
That Fig. 5 represents to be correlated with but with the described different embodiment of Fig. 4.In the design of Fig. 4, sectional or independent material feeding-passage are positioned at outside the passage OP, yet in the design of Fig. 5, independent feed material passage HMP1 and HMP2 are positioned at passage OP.Consideration for the possibility of the seepage of the thermostability of feed material and feeding-passage can influence the selection that designs between the embodiment of Figure 4 and 5.In the design of Fig. 4, steam is looped around around the independent feeding-passage, yet in Fig. 5, the source of oxygen gas-circulating is around it.
Fig. 6 represents another embodiment, and wherein the wall of nozzle N partly uses heat-eliminating medium source (for example water) to cool off, and this heat-eliminating medium source is from carry out round-robin source 14 by the passage WP that is incorporated into nozzle N.
Shown in Fig. 1-6, in the preferred embodiment of feed nozzle of the present invention, oxygen or Oxygen Flow mixture flow are through ending at the passage that contracts-expand of outlet orifice at the relief outlet of nozzle.The part that contracts-expand of nozzle is designed, thereby may obtain the ultrasonic flow of oxygen-containing gas at relief outlet.In preferred embodiments, the halogenated materials such as liquid RCl transmits by one or more second passages and the many relief outlets around the outlet orifice of oxygen-containing gas enter the ultrasonic wave air-flow.The relief outlet of liquefaction RCl preferably itself is the effluent streams that radially inwardly faces toward oxygen.As previously mentioned, the feed conduit of liquid RCl can divide or cut apart again, so that provide independent charging ability for the inconsistent different RCl of chemistry.
For the starting purpose, preferably use the centre pilot nozzle shown in Fig. 1,2,4 and 6 at the liquid feeding spray nozzle relief outlet (PDP) of nozzle downstream end with slower initial flow rate atomized feed.This is designed to provide guiding with charging slowly and oxygen rates pilot jet, and can be starting by the reactor that can add new incompatible logistics portative power is provided.
Can use independent pre-hot nozzle (not shown) that vapourizing furnace is heated to service temperature from the state of cooling, and in short RCl cut-off process holding temperature, simultaneously from heat operation attitude controlled chilling.Because a large amount of refractory substances by vapourizing furnace synthetic gas passage, therefore must controllably be introduced a large amount of heats, thereby refractory substance and gasification furnace chamber are heated to service temperature, preferably introduce liquid then.The thermal stresses that over-drastic heating or rate of cooling cause because of thermograde is damaged anti-RCl fire material.The function of preheat burner is very similar to described elementary vapourizing furnace and main jet or operation of combustors, and different is preferably different with the liquid RCl fuel gas of fuel.
For starting, small-sized guider at intermittence can be lighted preheat burner and heat refractory substance.Then fuel gas and oxygen are introduced and carried out external mix by preheat burner.After flow velocity reduces, can form stationary flame, the steam moderator is preferably with the mass ratio adding about 1: 1 with fuel gas.Oxygen and quality of fuel are than preferably being controlled at about 1.7: 1 to 2.0: 1 in starting process.It is slightly less than the required stoichiometry ratio of perfect combustion half.Maintain near 25 ℃/hour with the slow increase of flow velocity and with the refractory substance heating rate of controlling, be heated to required vapourizing furnace service temperature always.
Shown in Fig. 1-5, in certain embodiment preferred, this nozzle around RCl and oxygen channel for preferably with steam, CO
2And/or effective " rare gas element " that the form of water/halocarbon steam adds provides conduit.Optionally, rare gas element conduit on every side can be the conduit that adds methane or other fuel gas, with it as selectable added hydrogen and the extra fuel source that is used for reaction process.The gaseous state process steam stream of selecting is joined reactor to be replaced or increases steam or methane.This process steam stream is the non-oxidizable logistics that contains effective rare gas element, RCl or hydro carbons.In the rare gas element passage, can utilize coolant outlet, so that the surface portion of nozzle cools off by the thin cooling gas film that forms on the surface.Steam film refrigerative method is by shown in the Lefebvre (gas turbine combustion-1983).
The passage of nozzle (the particularly passage of the passage of oxygen source gas and halogenated materials) is constructed according to size, and working pressure, temperature and the steam flow rate in conjunction with expection obtains required outlet end speed simultaneously.Oxygen is preferred atomizing gas.Steam provides other or extra atomizing gas.
In the operation of routine, will 10 be fed to oxygen source gas passage OP from originating such as the oxygen source gas oxygen and/or steam and/or other oxygen source gas.The liquid halogenated materials is fed to the passage HMP (or passage HMP1 and HMP2) of halogenated materials from the source 11 of halogenated materials.Halogenated materials or fuel gas also optionally carry out fluid flow with the guide channel PP that contains charging other or that add.The design of nozzle makes oxygen source gas finally reach wave velocity at the expansion CV of the nozzle wall part that forms passage OP.The relief outlet DSE that expansion DV by nozzle wall part has found in adjacent nozzles expands oxygen source gas and preferably obtains ultrasonic velocity.Oxygen can disperse fully and atomize from the interior effusive liquid halogenated materials of relief outlet DP of the passage HMP (or passage HMP1 and HMP2) of halogenated materials with ultrasonic velocity.And, the halogenated materials such as RCl with such as O
2And so on the mixing of the oxygen source gas GR zone that should just in time in gasifying reactor, form in the downstream of nozzle N carry out.The design of chuck J1 helps effective rare gas element (for example steam) is discharged rare gas element along the nozzle wall part that forms the halogenated materials passage, the discharge end of contiguous halogenated materials, preferably pass or enter the relief outlet of halogenated materials, thereby the rare gas element curtain is provided.The relief outlet DP of the passage HMP of halogenated materials is advantageously constructed, thereby can partly radially inwardly discharge halogenated materials facing to the axle of nozzle.
In the starting process of nozzle, at first feed material preferably is fed to passage PP, flow out the terminal PT of directional nozzle by the relief outlet PDP in the directional nozzle PN then, the position of this directional nozzle and row's relief outlet and structure make it possible to temperature reactor 200 in reach treatment temp before, charging reach its operate flow velocity before and in the nozzle oxygen source gas begin gasification reaction before reaching wave velocity.In case reach technological temperature, pressure and speed, directional nozzle PN or successive or disconnection.
Extra fuel gas such as methane can be fed to the relief outlet DSE of nozzle N by the passage that chuck J2 partly forms.Steam as rare gas element can be discharged by the outlet V of chuck J1, thereby helps partly to provide the film cooling for wall part and the downstream end of nozzle N.
Fig. 9 represents the nozzle that can only dwindle.Expect this design and one expand design and have littler efficient, but do not reach preferred this design under the situation of ultrasonic velocity at oxygen than contracting.Except not having extended region, the structure of the designs of nozzles that can only dwindle and operate in the nozzle that main aspect is similar to Fig. 1-6.
About the selection of the building material of feed nozzle, should in given environment, find the canonical reference book and the document of appropriate structuring material.Preferred Hastelloy B or the C material of using.
Above-mentioned disclosure and description of the present invention are illustratives and indicative, can not depart from spirit of the present invention at size, shape and material and carrying out various variations aspect the details of illustrational system.The present invention utilizes and relies on the historical term of inferring to carry out the claim protection, has promptly described single composition and has covered one or more these key elements and two two or more these key elements of compositions covering.
Claims (27)
1. the combination of feed nozzle and gasifying reactor, this nozzle provides the first channel that contracts-expand, described passage ends at the outlet orifice of the downstream end that is positioned at described nozzle, and itself and oxygenous body source carry out fluid flow, is used for oxygen-containing gas is entered gasifying reactor; End at the second passage of at least one relief outlet with at least one downstream end at nozzle, the fluid supply of wherein said at least one second passage and halogenated materials carries out fluid flow, and the relief outlet of second passage radially is positioned at around the outlet orifice of first channel.
2. according to the described device of claim 1, wherein said nozzle provides the third channel of the relief outlet of at least one its relief outlet adjacent second passage, and described at least one third channel carries out fluid flow with effective inert gas source.
3. according to the described device of claim 2, wherein said rare gas element comprises steam, CO
2Or nitrogen.
4. according to the described device of claim 1, wherein said nozzle arrangements forms at least one circulation passage, and fluid flow is carried out in described at least one circulation passage and heat-eliminating medium source.
5. according to the described device of claim 2, the nozzle arrangements that wherein limits at least one second passage and at least one third channel makes the shared common wall of passage at least in part.
6. according to the described device of claim 3, wherein said nozzle arrangements provides outlet at the outer wall of at least one third channel.
7. according to the described device of claim 1, wherein said nozzle arrangements forms the four-way with relief outlet at the downstream end of nozzle, and described four-way and gas fuel source are carried out fluid flow.
8. according to the described device of claim 4, wherein said nozzle arrangements makes at least one circulation passage and the shared at least in part common wall of at least one second passage.
9. according to the described device of claim 2, wherein with the relief outlet structure of at least one third channel and be oriented with the relief outlet of at least one second passage and combine, so that the third channel relief outlet passes the relief outlet of second passage.
10. according to the described device of claim 1, it also comprises at least two second passages, and wherein said at least two second passages carry out fluid flow with independent halogenated materials fluid supply respectively.
11. according to the described nozzle of claim 1, wherein said at least one second passage relief outlet comprises the ring-type port around the outlet orifice that radially is positioned at first channel.
12. according to the described nozzle of claim 1, wherein said at least one second passage comprises that many ring-types are positioned at each first channel outlet orifice relief outlet on every side.
13., wherein described at least one second passage relief outlet is configured to radially inwardly carry out liquid discharge to small part according to the described device of claim 1.
14. according to the described nozzle of claim 1, wherein said nozzle arrangements also provides the directional nozzle that is positioned at first channel element, described directional nozzle element ends at outlet orifice at the downstream end of nozzle, and this directional nozzle element and gas fuel source are carried out fluid flow.
15. one kind is fed to method in the gasifying reactor with halogenated materials, this method comprises the oxygen source gas near sound wave or ultrasonic velocity is fed to the outlet orifice that enters the feed nozzle in the gasifying reactor; The liquid halogenated materials is discharged from the relief outlet that at least one radially is positioned at around the oxygen source gas of discharge, thereby enter and atomized liquid halogenated materials in gasifying reactor in the external oxygen source gaseous diffusion of feed nozzle at least.
16. in accordance with the method for claim 15, it comprises the discharge of the contiguous halogenated materials of effective rare gas element is discharged.
Comprise exhaust vapour 17. in accordance with the method for claim 16, wherein discharge effective rare gas element.
18. in accordance with the method for claim 15, it comprises that utilization cools off the outlet end of feed nozzle at least at the heat-eliminating medium of nozzle passage internal recycle.
19. in accordance with the method for claim 16, it comprise effective rare gas element through qualification the halogenated materials passage to small part wall and the rare gas element film that on wall, forms.
20. in accordance with the method for claim 17, it comprises from being limited to the outer wall that small part ground forms the rare gas element passage and discharges effective rare gas element.
21. in accordance with the method for claim 15, it comprises the downstream end of postcombustion gas at nozzle is drained in the gasifying reactor.
22. in accordance with the method for claim 16, it comprises effective rare gas element is discharged at the ejecta stream that the downstream end of nozzle passes halogenated materials.
23. in accordance with the method for claim 15, its outlet end that is included in nozzle is discharged at least two kinds of halogenated materials respectively.
24. a method of starting the gasifying reactor of halogenated materials, this method are included in the outlet orifice supply oxygen source gas of the feed nozzle that enters gasifying reactor; Downstream end at nozzle in the oxygen source gas of discharging is discharged the fuel gas logistics; And in nozzle, the speed of oxygen source gas is increased to wave velocity.
25. in accordance with the method for claim 24, it comprises when oxygen source gas during near wave velocity, radially is positioned at relief outlet expel liquid halogenated materials little by little around the oxygen source gas of discharge from least one.
Combine with gasifying reactor and be suitable for being connected to nozzle on the gasifying reactor of halogenated materials 26. a feed nozzle, this nozzle comprise; This nozzle provides
End at the first channel that dwindles of the outlet orifice that is positioned at the nozzle downstream end, and it is configured to enter gasifying reactor;
The gas source of described first channel and oxygen is carried out fluid flow;
At least one second passage ends at least one relief outlet at the downstream end of nozzle;
Fluid flow is carried out in described at least one second passage and liquid halogenated materials source, and its relief outlet radially is positioned at around the outlet orifice of first channel; With
The third channel of the relief outlet of at least one its relief outlet adjacent second passage, described at least one third channel carries out fluid flow with effective inert gas source.
27. according to the described device of claim 26, wherein said nozzle arrangements defines the fuel gas passage that has relief outlet at the downstream end of nozzle, described fuel gas passage and fuel gas source carry out fluid flow.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US56617600A | 2000-05-05 | 2000-05-05 | |
| US09/566,176 | 2000-05-05 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1439044A true CN1439044A (en) | 2003-08-27 |
| CN1260001C CN1260001C (en) | 2006-06-21 |
Family
ID=24261823
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 01808843 Expired - Fee Related CN1260001C (en) | 2000-05-05 | 2001-05-04 | Feed nozzle for gasification reactor for halogenated materials |
Country Status (10)
| Country | Link |
|---|---|
| EP (1) | EP1287094A2 (en) |
| JP (1) | JP2003532535A (en) |
| CN (1) | CN1260001C (en) |
| AU (1) | AU2001261201A1 (en) |
| BR (1) | BR0110335A (en) |
| CA (1) | CA2406540A1 (en) |
| MX (1) | MXPA02010886A (en) |
| NO (1) | NO20025287L (en) |
| RU (1) | RU2002132654A (en) |
| WO (1) | WO2001085873A2 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102373094A (en) * | 2010-08-11 | 2012-03-14 | 通用电气公司 | Apparatus for removing heat from injection devices and method of assembling same |
| CN101848902B (en) * | 2007-12-14 | 2012-08-29 | 陶氏技术投资有限公司 | Wet scrubbing for removing particulate solids from oxygen supply line |
| CN109609194A (en) * | 2018-12-27 | 2019-04-12 | 西安元创化工科技股份有限公司 | A kind of slurry and oxygen feeding control method of multi-channel nozzle |
Families Citing this family (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100441945C (en) * | 2006-09-27 | 2008-12-10 | 华东理工大学 | Beaming type gasification or combustion nozzle and its industrial use |
| WO2009078899A1 (en) | 2007-12-14 | 2009-06-25 | Dow Technology Investments Llc | Oxygen/hydrocarbon rapid (high shear) gas mixer, particularly for the production of ethylene oxide |
| WO2009078898A1 (en) * | 2007-12-14 | 2009-06-25 | Dow Technology Investments Llc | Hydrocarbon/oxygen industrial gas mixer with coarse water droplet environment to reduce ignition potential |
| US8404190B2 (en) | 2007-12-14 | 2013-03-26 | Dow Technology Investments Llc | Hydrocarbon/oxygen industrial gas mixer with water mist |
| WO2009102311A2 (en) | 2007-12-14 | 2009-08-20 | Dow Technology Investments Llc | Low shear gas mixer |
| US9023121B2 (en) | 2010-10-20 | 2015-05-05 | Alliant Techsystems Inc. | Solid feed systems for elevated pressure processes, gasification systems and related methods |
| US8795602B2 (en) * | 2011-09-29 | 2014-08-05 | General Electric Company | Multi-stream feed injector |
| CN109504457B (en) * | 2017-09-15 | 2024-04-16 | 通用电气神华气化技术有限公司 | Impact type mixing atomization device and method |
| CN109210531B (en) * | 2018-10-19 | 2023-11-10 | 宁夏神耀科技有限责任公司 | Liquid fuel efficient combined burner for pressurized gasification furnace |
| CN113150831B (en) * | 2021-04-19 | 2022-08-26 | 哈尔滨工业大学 | Protection device for ejector nozzle and use method |
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| US3305309A (en) * | 1963-03-25 | 1967-02-21 | Hooker Chemical Corp | Production and recovery of hydrogen halides |
| BE776576A (en) * | 1971-12-10 | 1972-04-04 | Centre Rech Metallurgique | OXYGEN BURNER, |
| JPS5233380A (en) * | 1975-09-08 | 1977-03-14 | Kanto Denka Kogyo Kk | Sludge like organic matter furnace |
| US4353712A (en) * | 1980-07-14 | 1982-10-12 | Texaco Inc. | Start-up method for partial oxidation process |
| US4857075A (en) * | 1988-05-19 | 1989-08-15 | The Dow Chemical Company | Apparatus for use with pressurized reactors |
| US5129335A (en) * | 1991-04-18 | 1992-07-14 | Union Carbide Industrial Gases Technology Corporation | Fluid waste burner system |
| US5261602A (en) * | 1991-12-23 | 1993-11-16 | Texaco Inc. | Partial oxidation process and burner with porous tip |
| US5599375A (en) * | 1994-08-29 | 1997-02-04 | American Combustion, Inc. | Method for electric steelmaking |
| CN1332877C (en) * | 1997-12-22 | 2007-08-22 | 陶氏环球技术公司 | Prodn. of one or more useful products from lesser value halogenated materials |
-
2001
- 2001-05-04 WO PCT/US2001/014497 patent/WO2001085873A2/en active Application Filing
- 2001-05-04 CA CA002406540A patent/CA2406540A1/en not_active Abandoned
- 2001-05-04 AU AU2001261201A patent/AU2001261201A1/en not_active Abandoned
- 2001-05-04 MX MXPA02010886A patent/MXPA02010886A/en not_active Application Discontinuation
- 2001-05-04 CN CN 01808843 patent/CN1260001C/en not_active Expired - Fee Related
- 2001-05-04 JP JP2001582463A patent/JP2003532535A/en active Pending
- 2001-05-04 EP EP01935075A patent/EP1287094A2/en not_active Withdrawn
- 2001-05-04 RU RU2002132654/12A patent/RU2002132654A/en not_active Application Discontinuation
- 2001-05-04 BR BR0110335-0A patent/BR0110335A/en not_active Application Discontinuation
-
2002
- 2002-11-04 NO NO20025287A patent/NO20025287L/en not_active Application Discontinuation
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101848902B (en) * | 2007-12-14 | 2012-08-29 | 陶氏技术投资有限公司 | Wet scrubbing for removing particulate solids from oxygen supply line |
| CN102373094A (en) * | 2010-08-11 | 2012-03-14 | 通用电气公司 | Apparatus for removing heat from injection devices and method of assembling same |
| CN102373094B (en) * | 2010-08-11 | 2014-11-26 | 通用电气公司 | Apparatus for removing heat from injection devices and method of assembling same |
| US9303221B2 (en) | 2010-08-11 | 2016-04-05 | General Electric Company | Apparatus for removing heat from injection devices and method of assembling same |
| CN109609194A (en) * | 2018-12-27 | 2019-04-12 | 西安元创化工科技股份有限公司 | A kind of slurry and oxygen feeding control method of multi-channel nozzle |
| CN109609194B (en) * | 2018-12-27 | 2020-12-15 | 西安元创化工科技股份有限公司 | Slurry and oxygen feeding control method of multi-channel nozzle |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2001085873A2 (en) | 2001-11-15 |
| WO2001085873A3 (en) | 2002-11-28 |
| NO20025287L (en) | 2002-12-20 |
| CA2406540A1 (en) | 2001-11-15 |
| NO20025287D0 (en) | 2002-11-04 |
| AU2001261201A1 (en) | 2001-11-20 |
| JP2003532535A (en) | 2003-11-05 |
| BR0110335A (en) | 2003-12-30 |
| RU2002132654A (en) | 2004-04-20 |
| CN1260001C (en) | 2006-06-21 |
| MXPA02010886A (en) | 2004-09-06 |
| EP1287094A2 (en) | 2003-03-05 |
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