CN86102626A - The use technology and the device of pressurized reactor - Google Patents

The use technology and the device of pressurized reactor Download PDF

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Publication number
CN86102626A
CN86102626A CN86102626.8A CN86102626A CN86102626A CN 86102626 A CN86102626 A CN 86102626A CN 86102626 A CN86102626 A CN 86102626A CN 86102626 A CN86102626 A CN 86102626A
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China
Prior art keywords
burner
pipe
oxygen
gas
carbon containing
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CN86102626.8A
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CN1010027B (en
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查理斯·W·利普
道格拉斯·D·马里克
理查德·A·利
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Dow Chemical Co
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Dow Chemical Co
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Publication of CN86102626A publication Critical patent/CN86102626A/en
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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
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/12—Heating the gasifier
    • C10J2300/1223—Heating the gasifier by burners

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Industrial Gases (AREA)

Abstract

The invention relates to a kind of technology burner, be used for simultaneously and selectively carbon containing slurry, oxygen-containing gas, fuel gas and optional temperature slowed down agent being added to part pressure oxidation district.These burner characteristics are that the interior homogeneous dispersion of carbon containing slurry is introduced oxygen-containing gas and high atomization dispersibility carbon contained silt material.The other characteristics of technology burner are from the outside of technology burner, the dispersion of fuel gas to be introduced in the oxygen-containing gas.

Description

The use technology and the device of pressurized reactor
The invention relates to the method for pressurized reactor input fluid foods.The invention still further relates to the device that to implement this course of conveying.From concrete aspect: the method that method and apparatus of the present invention relates to by the high-pressure section oxidation of carbon containing slurry prepares hydrogeneous (H 2) and the gaseous product of carbon monoxide (CO), for example: synthetic gas, reducing gas and fuel gas.
In present technique, the technology and the wherein employed device of the oxidation of carbon containing slurry high-pressure section all are well-known.For example, referring to United States Patent (USP) 4113,445; 4,353,712 and 4,443,230.In most of examples, carbon containing slurry and oxygen-containing gas add in the reactor, and this reactor is about 2500 °F (1370 ℃) usually on the volatilization temperature of the devolatilization product that is in the carbon containing slurry in the presence of the oxygen.By at least two kinds of methods, just can be heated to auto ignition temp to reactor.One of this method is: air tight manner is fixed on the interface of reactor burner beyond the simple preheat burner.This preheat burner is fuel gas, for example: methane, being defeated by reactor is enough to the high temperature that reactor heating reaches about 2000～2500 ℃ (1090～1370 ℃) with generation, the heat-stable material that the heat-up rate that is adopted can not the damaging reaction device.Usually, above-mentioned heat-up rate is about 40 ℃/hr～80 ℃/hr(44 ℃/hr～27 ℃/hr).In pre-heating step, reactor remains on ambient pressure or hangs down the pressure of some a little than it.Be lower than extraneous pressure and meet the requirements, because it can make air enter reactor by the outer resistance to air loss connecting portion between preheater and the reactor, this air is used for combustion fuel gas then.After the preheating temperature of needs reaches, change preheat burner from reactor, replace the technology burner.Because in the replacing time.Reactor will can cool down gradually, thus above-mentioned more get in return fast as much as possible.Generally speaking, be cooled to the low temperature of 1800 (980 ℃).If the temperature of reactor still is in the suitable temperature range, carbon containing slurry, oxygen-containing gas and be with or without temperature and slow down agent and be sent to the technology burner and carry out the slurry partial oxidation.Importing slurry at the beginning must light the oxygen-containing gas of input, so that apace the reaction zone heating is reached on the temperature of reaction zone generation slag.Above-mentioned rapid heating process can produce thermal shocking to the refractory materials of reactor.
Yet,, so just must use preheater again if the temperature of reactor is too low.Because device repeats to change and causes process period waste and at the labour cost at the volume of cost place, so this replacing does not meet the requirements.
Another that reactor is heated in the employed two kinds of methods of temperature range of expection only requires to use the technology burner; For example, referring to disclosed burner in the United States Patent (USP) 4353,712.The technology burner of this type is provided for the carbon containing slurry, oxygen-containing gas, fuel gas and/or temperature slow down agent optionally respectively with the conduit of while charging.When this technology burner is used for when preheating reactor, this burner is imported oxygen-containing gas and combustion gases in the proper ratio so that fully burning.After reactor reached desired temperature range, fuel gas both can be replaced fully by the carbon containing slurry also can be co-fed with slurry.If adopt co-fed mode, to reduce the charging of fuel gas so usually, so that only produce the part oxygenizement.When in reactor, failing the carbon slurry at first and keeping the temperature of reactor, adopt co-fed mode usually, until the process conditions balance of carbon containing slurry/oxygen-containing gas feed operation state.
Though only use technology operation of combustors mode not have the waste of the sort of process period of pre-heaters/technology operation of combustors mode and the shortcoming of extra investment in human resources, it is not impeccable itself.When only using technology operation of combustors mode, be difficult to keep flame stability fully under environmental stress oxidation and two kinds of conditions of high-pressure section oxidation, and can also reduce reliability of technology, these two kinds of conditions are respectively applied for the processing step that preheats with carbon containing slurry partial oxidation.
In synthetic gas industry, some people has advised adopting the operating method that preheats burner and technology burner and usefulness, and wherein the latter can provide carbon containing slurry, oxygen-containing gas, fuel gas and/or temperature to slow down optionally charging simultaneously of agent.Though it is this and still can produce owing to the technology burner is changed the process time that pre-burners brings and the waste of labour cost with mode, but the characteristics of technology burner charging when selecting have but reduced the thermal shock problem to the reactor refractory materials of above-mentioned discussion.By input fuel device gas reaction gas temperature temperature after its cooling is brought up to preset temperature, then adopt carbon containing slurry and fuel gas simultaneously the operating method of feed to reach the purpose of minimizing thermal shocking.The carbon containing slurry begins with the charging of low amount, then when the feeding coal of fuel gas zero and increase other inlet amount along with reactor being gradually reduced to of keeping that self preset temperature institute must heat.Because beginning is supplied with the carbon containing slurry with low rate, so less slurry heating and evaporation are arranged, like this, the decline of temperature of reactor is minimum.In addition, at the initial stage of carbon containing slurry feeding, the continuously feeding meeting of fuel gas causes adding heat to reactor.Fuel gas burns under the condition of partial oxidation does not have gaseous product, (for example: pollution problem carbonic acid gas).
Because the technology burner in the program of just having described uses effectively, so it must offer reactor to carbon containing slurry and fuel gas thing with their oxygen-containing gas materials separately with efficient manner.Process efficiency requires the carbon containing slurry to be evenly dispersed in the oxygen-containing gas and presents the atomizing state of height, and for example: the particle diameter that drop had is less than about 1000 microns.Disperse uniformly and atomizing all help guaranteeing fully to burn and avoid in reaction zone, producing partial overheated.
The invention provides a technology burner, it can be the stream of the material liquid more than three kinds or three kinds and also offers reaction zone simultaneously respectively, and can make the atomizing of carbon containing slurry homodisperse ground simultaneously in oxygenous.
The invention provides a kind of novel technology burner, it is used for partial oxidation by a container carbon containing slurry and is used for preparation and can becomes gas, fuel gas, or reducing gas.This container provides a reaction zone, and its pressure range is maintained at about 15～3500PSig(0.2～24MPa) usually, and the best is about 1500～2500PSig(10.4～17.3MPa) and its temperature range is about 1700～3500 ℃ (930～1930 ℃).Burner is installed on the container, and carbon containing slurry, oxygen-containing gas and temperature are slowed down agent (selecting for use arbitrarily) and be sent to reaction zone by burner whereby.In addition, burner also offers a kind of fuel gas of reaction zone, for example: methane, fuel device can be respectively with handle all these material liquid streams simultaneously.
So it can provide carbon containing slurry that high atomisation forms to reaction zone because technology burner of the present invention has unique appearance, both the volume averaging size droplet diameter scope that has of carbon containing slurry was about 100～600 microns.When carbon containing slurry and oxygen-containing gas entered reaction zone, the carbon containing slurry was not only by high atomisation, and it also is evenly dispersed in the oxygen-containing gas fully.Because burner can make the dispersion atomizing evenly, can obtain very uniform burning so make in reaction zone.The technology burner of prior art can not guarantee the atomizing and the dispersity of carbon containing slurry and oxygen-containing gas, and it can produce non-uniform combustion thus, the byproduct that local superheating and not wishing obtains () problem for example: carbon or carbonic acid gas.It also is important feature of the present invention that homodisperse and atomizing occur in nozzle interior.After the carbon containing slurry fully disperses and atomizes, after in reaction zone, fully disperseing and atomizing, before the reaction zone internal combustion, the degree of atomization of strict control carbon containing slurry in nozzle.The nozzle of prior art was once attempted to promote whole, both made not to be whole, the atomizing in the reaction zone, but along with further atomizing is compelled to occur in (both in the reaction zone) in the zone, they just can not control particle diameter, say that by the atomizing standard this is unconfined.Atomization process in the reaction zone is also relevant with the oxygen-containing gas burning competition time with the carbon containing slurry.
Technology burner another one characteristics of the present invention are fuel gas is sent to reaction zone, and fuel gas to be from outside input technology burner.One of benefit of the outside input of fuel gas is: the flame of fuel gas can keep certain distance with burner surface.If burning bluster will be damaged burner so near burner surface.If the oxygen (O in the oxygen-containing gas 2) the content height ratio is as 50%, the inside input from the technology burner does not meet the requirements fully so, is very fast because expand at the flame of the high fuel gas of oxygen content.Like this, will exist expansion to cause the danger of burner badly damaged owing to flame in the burner.
When burner is used to prepare H 2During with CO, just can improve technology.Contain in the technology of H and CO gas in partial oxidation preparation by the carbon containing slurry in the container, this container provides a reaction zone, its pressure range maintain usually about 15～3500PSig(0.2～24MPa) with and about 1700～3500 of temperature range (930～1930 ℃), improvements comprise:
A. carbon containing slurry and oxygen-containing gas as reactant are imported above-mentioned reaction zone, before above-mentioned reactant entered above-mentioned reaction zone, above-mentioned carbon containing slurry extremely was evenly dispersed in the oxygen-containing gas and atomizing.
B. send into above-mentioned reaction zone keeping above-mentioned reaction zone at the needed fuel gas of said temperature, make above-mentioned fuel gas and enter the reactant thorough mixing, above-mentioned fuel gas is directly sent to reactant in (a) step;
C. by the partial oxidation effect, make the reaction of (a) step in above-mentioned reaction zone and generate by H 2Gas with the CO composition; And
D. by the partial oxidation effect, the oxygen-containing gas reactant of introducing in above-mentioned (a) step with the fuel gas of a certain amount of introduction of above-mentioned (b) step and at least a portion reacts.
Technology burner in the example of the present invention (as shown in Figure 1) has can provide a center circle tubular oxygen flow, ring-type to contain a slurry flow and a year coniform oxygen flow.These air-flows mutually with one heart and the heart and radially transmitting mutually so that central gas stream be in round shape oxygenous in and round shape carbon containing slurry flow at a certain angle (its scope is about 15 °～75 °) mix with frusto-conical is oxygenous.The scope of oxygen flow flow velocity is about 75 feet per seconds (23 meter per second)～velocity of sound and greater than the flow velocity of carbon containing slurry flow, its lowest speed is about 1 feet per second (0.3 meter per second).By adjusting fluid and their different in flow rate, just can make carbon containing slurry dispersion very equably in the oxygen-containing gas.
Frusto-conical and the oxygen flow center circle tubular all can shearing cylinder shape slurry flows and slurry is disperseed and begin atomizing.After disperseing and beginning atomizing, the dispersion of slurry and gas is by an acceleration zone.Situation is such in first example just as discussed above, flows hollow vertical cylinder conduit by near the liquid downward summit that is positioned on the frustoconical air-flow, can form acceleration zone.For above-mentioned example, the sectional area of hollow cylinder conduit less than the cylinder carbon containing become silted up adding of stream, three sectional areas of center drum frusto-conical oxygen flow and.The processing of this hollow cylinder conduit and the foundation of finish size and above-mentioned the same described in the example of first technology burner.
As the specific examples of first technology burner, this technology burner provides dyestuff gas to reaction zone, for the dispersion that makes the carbon containing slurry/oxygen-containing gas in reaction zone is disperseed.This dye-gas dissemination is to carry out in the inside of technology burner.
The burner structure that above-mentioned example of the present invention provides consists of:
(a) the hollow cylinder centre pipe is taked overhead stream feed and underfeed mode.
(b) the first layer cylindrical duct is coaxial and surround the above-mentioned centre pipe of certain-length at least with described centre pipe, and above-mentioned the first layer cylindrical duct is taked top fluid feed and underfeed mode.
(c) second layer cylindrical duct is coaxial with the first layer cylindrical duct, and surrounds the above-mentioned round conduit of certain-length at least, and takes overhead stream feeding material and underfeed mode.
(d) sectional area of hollow garden shape acceleration duct less than the sectional area of above-mentioned centre pipe, the first layer garden tube conduit and second layer garden tube conduit add and, and have opening for feed near end at the outer side of said burner.
(e) the butt conical surface is connected with the top of acceleration duct at its top, and directly is connected with above-mentioned second layer cylindrical duct bottom outside in its bottom; And
(f) having the outer side import of a gas duct and said burner at least is fluid transmission.
In order to make carbon containing slurry homodisperse in oxygenous, another device of the present invention has technology incendiary characteristics, and as shown in Figure 2, its structure can provide the frustoconical oxygen flow of first speed of generation.Another burner structure provides the round shape carbon containing slurry stream of second speed.Purpose with round shape liquid stream feed is that it is crossing with the internal surface of the truncated conelike air-flow of oxygen-containing gas.The preferable range that intersects angle is about 15 °～75 °.The preferable range of truncated conelike air-flow velocity is about 75 feet per seconds (23 meter per second)～velocity of sound, and should be greater than preferred carbon containing slurry liquid flowing speed, and its scope is about 1～50 feet per second (0.3～15 meter per second).
Crossing and by round shape carbon containing slurry stream and frusto-conical oxygen flow by the difference between two kinds of rate of flow of fluids, just can from technology nozzle of the present invention, spray very uniform dispersion.Yet can believe that technology burner of the present invention is not limited to foregoing: the frusto-conical air-flow is sheared and partly atomized round shape slurry stream at least.
After obtaining desired homogeneous dispersion, the carbon containing slurry will further atomizing in the technology burner.This further atomizing preferably obtains by the acceleration zone mode by dispersive slurry and gas.This acceleration zone is near form Frusto-conical fluid top preferably; Be equipped with conduit under the hollow cylinder, its net sectional area less than the net sectional area of round shape carbon containing slurry flow and butt cylinder oxygen flow add and.Intersection at the top of frustoconical top and acceleration duct records pressure P 1, keep the pressure P that records near end inside greater than at acceleration zone 2P 1-P 2Pressure difference preferably remain in 10～1500psi(0.2～10.4MPa).According to hydromeehanics law and the excessive hypothesis of stable liquid circulation, two kinds of fluids are along with they will be accelerated by cylindrical duct.The diffusing fluidic gas ratio slurry components of a part quickens more comparatively fast, makes that like this slurry drop is further sheared, and slurry is atomized thinlyyer.The degree that the length of cylinder acceleration duct and diameter carry out for atomizing plays conclusive effect at least partially.The diameter and the length of acceleration duct depend on P 1-P 2The temperature, the relative quantity of use, slurry and gas that temperature is slowed down agent or the like of pressure reduction, slurry viscosity, slurry and gas.Though have many variablees that connect each other, the test determination of acceleration duct diameter and length is necessary.
The characteristics of burner provided by the invention are:
(a) fluid material inlet and the hollow cylinder centre pipe of opening for feed is arranged in its bottom is arranged at its top;
(b) the first layer cylinder conduit is coaxial and surround the above-mentioned conduit of certain-length at least with above-mentioned conduit;
(c) net sectional area add less than the free area of above-mentioned centre pipe and above-mentioned the first layer cylinder conduit and the hollow cylinder acceleration duct, and have nearly material mouth at the survey face of top feed and above-mentioned fuel device at it;
(d) fi-ustoconical surface is connected with the top of above-mentioned acceleration duct at its top, and is connected with the terminal external diameter of above-mentioned the first layer cylindrical duct in its bottom; And
(e) have at least the opening on the shell of a gas duct and said burner to carry out the fluid transmission.
Technology burner of the present invention is specially adapted to the non-catalytic partial oxidation technology air-flow that processes raw material in reaction zone, reaction zone is made of the refractory liner container.The technology burner both can temporarily also can for good and all be installed on the opening of container burner.When having only preheat burner for good and all to be installed on the container, just for good and all install burner, in this case, after tapping into preheater and making it reach initial reaction district temperature, disconnect preheat burner, preheat burner is followed technology burner of the present invention and is started working after disconnecting.The temporary transient installation of technology burner is used for following situation; After initial heating, take off preheat burner, change the technology burner.
As previously mentioned, the partial oxidation reaction of the carbon containing slurry of preparation synthetic gas, fuel gas or reducing gas usually occurs in the reaction zone, its temperature range is about 1700～3500 °F (930～1930 ℃), and its pressure range is about 15～3500psig(0.2～24MPa).United States Patent (USP), 2,809,104, middle typical partial oxidation reaction producer gas generator described.The air-flow major part that is produced contains hydrogen and carbon monoxide also can contain one or more following component: CO, N 2O, N 2, Ar, CH 4, H 2S and COS.According to obtaining fuel and employed operational condition, flow of feed gas also can contain inclusion, for example fine grain carbon black, flash distillation thing or slag.Constantly remove then from here the bottom that part acetonitrile technology slag that generate and that flow of feed gas is carried secretly will be fallen container.
Term used herein " carbon containing slurry " means the slurry of carbonaceous solids pigment, its pumpable material; Usually its solids content scope is about 40%～80%, and it can be by the conduit of the hereinafter described technology nozzle of the present invention.Above-mentioned slurry is normally by fluid carrier and solid carbon fuel mix.Fluid carrier both can be a water, fluid or hydrocarbon thing, perhaps their mixture.Water is preferred carrier.Example as the hydrocarbon thing of liquid of useful carrier is as follows: liquefied petroleum gas (LPG), petroleum distillate and residue, gasoline, petroleum naphtha, kerosene, crude oil, pitch, gas oil, Residual oil, tar, husky oil, shale oil, coal extract oil, coal tar, process by-product oxygen-bearing liquid hydrogen compound and their mixture and the aromatic hydrocarbon that extract again, methyl alcohol, ethanol, other alcohols carbonyl and the hydroxyl building-up reactions of circulation diesel oil, coke or the diesel oil produced obtain from fluid catalytic cracking, for example: benzene, toluene and dimethylbenzene.Another liquid vehicle is a Liquid carbon dioxide.In order to guarantee that the carbonic acid gas carrier is a liquid state, carbonic acid gas adds the temperature range of technology burner should be decided according to pressure at about-67～100 (35～40 ℃).According to reports, when using Liquid carbon dioxide, liquid slurry contains has an appointment 40～70(by weight percentage) amount of being is good.
Usually solid carbon fuel comprises coal, coal tar, coal, gelatin liquefaction residue, petroleum coke, particulate state carbon black, tar sand or pitch from resinous shale derivative solid.Because hard coal, bituminous coal, sub-bituminous coal and brown coal can both use, so the kind of used coal is not key factor usually.The example of other solid carbon fuel is: the waste material of pulverizing, the sewage rubbish of dehydration and semi-solid organic materials, for example: pitch, rubber and rubber like material (rubber tyre that comprises automobile).As mentioned above, the carbon containing slurry that is used for technology burner of the present invention can be taken out with pump, and can pass through the conduit of the technology burner of design.In order to reach this purpose, the solid carbon fuel component of slurry will grind, so that all materials can be by one in fact: the 140mm sieve (can select sieve for use No. 14) of ASTM EH-170 ℃ of dusting cover stdn rule, and at least 80% material can sieve (can select sieve for use No. 40) by the 425mm of an ASTM E11-170 ℃ dusting cover standard code.Measure sieve aperture with solid carbon fuel, its moisture content scope is about 0～40(weight percentage).
Employed oxygen-containing gas can be an air in the technology burner of the present invention, and oxygen-rich air (being the air of oxygen level greater than 20 molecular fractions) also can be a pure oxygen.
As mentioned above, temperature is slowed down agent and be can be used for main technology burner.Said temperature slows down agent and mixes use with carbon containing slurry flow and/or oxygen flow usually.The example that the temperature that is suitable for is slowed down agent is the recycling part of the partial oxidation technology generation gas of water, fluid, carbonic acid gas, nitrogen and description herein.
The outer fuel gas of discharging of main technology burner comprises such class gas, for example: methane, ethane, propane, butane, synthetic gas, hydrogen and Sweet natural gas.
The characteristics of the polymolecularity of technology burner of the present invention and high fog voltinism and other can impel the characteristics of technology burner in the effect of application and economic aspect acquisition satisfaction, will clearer understanding be arranged to them so with reference to relation (wherein same numbers refers to identical parts) between the following accompanying drawing.
In the accompanying drawing:
Fig. 1 is the vertical sectional view of a technology burner of the present invention;
Fig. 2 is the vertical cross section of another technology burner of the present invention;
Fig. 3 is the sectional view of 3-3 line segment intercepting from Fig. 1; And
Fig. 4 is the sectional view of 4-4 line segment intercepting from Fig. 2.
With reference to figure 1 and 3, can see one herein usually with the numeral 10 technology burners of indicating of the present invention.By allowing the dirty end of technology burner 10 be passed down through the open pore of a partial oxidation syngas reactor, insert the technology burner.Technology burner 10 positions be in reactor head or or be in its side, this depends on the configuration of reactor.The technology burner both can forever have been installed also and can temporarily install, and this depends on whether can use together with the permanent burner of installing, perhaps be used to change preheat burner, all modes as previously mentioned.Utilize annular flange 48, install technology burner 10.
Technology burner 10 has the pipe 22 of a center configuration, and its top is sealed by plate 21, and is the frustoconical wall 26 of shrinking in the bottom.On the summit of frustoconical wall 26 are openings 35, and it and acceleration zone 33 carry out the fluid transmission.Acceleration zone 33 in the specific examples shown in the drawings is hollow just columnar districts.By and with the hole of plate 21, what be tightly connected is carbon containing slurry supply pipe 14.The least significant end of carbon containing slurry supply pipe is connected with annular plate 17, the upper end of annular plate 17 enclose dispenser 16.Divider 16 has the low wall 19 of the conical butt of a contraction.The top of frustum of a cone wall 19 is sag pipes 28, and it limits the external world of slurry conduit 25.The internal diameter of pipe 28 requires to be significantly smaller than the internal diameter of distribution piping 16.Can find, utilize divider 16, from the carbon containing slurry flow that the opening that is positioned at conduit 25 sprays, be very uniform in its annular extent.Determine the internal diameter of distribution piping 16 and pipe 28, so as along with the carbon containing slurry by managing 28 inwall and managing pressure that annular pipe 25 that 23 outer wall surrounds produced and fall pressure reduction between the highest and minimal pressure that will substantially exceed the slurry of measuring on distribution piping 16 inner arbitrary annular horizontal sections.As will be explained hereinafter, if the untenable words of this pressure dependence can be found: annular pipe 25 can produce unsettled hoop and flow; And when the carbon containing slurry contacts with the conical butt oxygen flow, will cause the decline of dispersion efficiency.
The external diameter of annular pipe 25 and difference in internal diameters depend on the fineness of the carbon containing slurry in the slurry at least in part.Annular pipe diameter difference should be even as big as preventing the carbonaceous material particle plugging in the used slurry.In many application, external diameter difference scope is about 0.1～1.0 inch (0.2～2.5 centimetre) in the annular pipe 25.
Co-axial with divider 16 and sag pipe 28 is pipe 23, and its diameter is all very even from top to bottom.Pipe 23 provides a pipe 27 as the oxygen-containing gas passage, and not only its upper reaches end and dirty end are open, and dirty end opening is wanted complete coplane with the dirty end opening of pipe 28.
By supply pipe 24, oxygen-containing gas is sent into technology burner 10.Part oxygen-containing gas is by the opening of pipe 23 and by conduit 27.The oxygen-containing gas of rest part flows through pipe 22 interior pipe and manages annular pipe 31 between 28 the outer wall.Along with oxygen-containing gas is forced through frustoconical conduit between the butt conical surface 26 and 20, this gas will be accelerated.Gap between the butt conical surface 20 and 26 can provide from carbon containing slurry conduit 25 effusive carbon containing slurry and effectively disperse required oxygen-containing gas flow velocity.For example, have been found that, if oxygen-containing gas with the calculating flow velocity of about 200 feet per seconds by conduit 27 and carbon containing slurry with the flow velocity of about 8 feet per seconds during by conduit 25 and their inner and outer diameter difference be about 0.3 inch (7.6 centimetres), oxygen-containing gas will be with the calculating flow velocity of about 200 feet per seconds by the frustoconical conduit so.In general, for just reading and the following fluid that will speak of, the gap on two frustum surfaces is at about 0.05～0.94 inch (in 0.13～2.4cm) the scope.With regard to these fluids and relative rate, have been found that the height of acceleration zone and diameter should be respectively 7 inches (17cm) and about 1.4 inches (3.6cm).
Butt periphery 26 is prolonging the prolongation longitudinal axis that the interior angle of about 15 °～75 ° scopes converges at pipe 28.If angle is too little, such as 10 °, then oxygenous impact surface causes very big energy consumption, if but angle is too little, and then the shearing action of Huo Deing is too little again.
Cast water jacket 32 is concentric with pipe 22, seals at the water jacket topmost by ring-like plate 58.Water jacket 32 foots are annular plates 42, and it is expanded inwards, constitute ring-like water route 43.Annular space between the outer wall of pipe 22 and the inwall of water jacket 32 has three fuel channels 36,40 and 41 to constitute by managing 36a and 40a and 41a respectively.As shown in Figure 1, pipe 36a, 40a and 41a pass the hole in the flange 42.Fuel gas is respectively by feed- pipe 52 and 50, through pipe 40a and 36a air feed.Do not express the feed-pipe that is used to manage 41a among the figure, but it and employed other tubing has same-type.
As shown in Figure 1, fuel gas passage 40 is identical with fuel gas passage 41 with 36() with pipe 28 longitudinal axis extension line at angle.On above-mentioned coaxial direction, passage isogonism and arranged spaced equidistantly radially, this angle and gap are the most useful, because it is behind ostium 30, and the direct dispersion of fuel pneumatic transmission carbon containing slurry/oxygen-containing gas equably.Should select the angle of fuel gas passage like this: at the distance burner surface fuel gas of introducing enough far away, but can not be as far as hindering fuel gas and carbon containing slurry/oxygen-containing gas fluid short mix or dispersion.Generally speaking, angle a as shown in Figure 1 1And a 2Should be in about 30 °～70 ° scope.
Burner housing 44 is installed with one heart and is radially moved outside water jacket 32 outer walls.Looping aquaporin 45 is outwards moved in the footpath of burner housing 44.The upper end of burner housing is equipped with water shoot 56.As shown in Figure 1, the water through water inlet pipe 54 enters flows through aquaporin 43, passes through ring-shaped water jacket 45 therefrom, discharges from water shoot 56.These current are used for keeping technology burner 10 in needed substantially invariable temperature.
With annular flange 60, with watertight means, sealing burner housing 44 upper ends.Burner housing 44 foots are burner end faces 46.
Down, reaction zone is finished after the pre-heating stage in working order, the temperature of reaction zone is risen in the preferable range of about 1500～2500 (810～1370 ℃), and technology burner 10 is introduced pipeline.Careful control liquid material and the relative proportion of slowing down agent through the optional temperature of technology burner 10 introducing reaction zones are so that the carbon of major portion transforms required product gas composition CO and H and keeps suitable temperature of reaction in carbon containing slurry and the fuel gas.
After the liquid material left technology burner 10, its residence time in reactor was about 1～10 second.
Oxygen-containing gas according to its oxygen level at a certain temperature, and is reinforced to technology burner 10.With regard to air, temperature from envrionment temperature to about 1200 °F (650 ℃); And for pure oxygen, temperature is from about envrionment temperature to 800 °F (427 ℃).Under the pressure of about 30～3500psig(0.3～24Mpa), the input oxygen-containing gas.Under the temperature and pressure of liquid vehicle temperature of saturation and about 30～3500psig(0.3～24Mpa), import the carbon containing slurry in about envrionment temperature.Be used to keep the fuel gas of reaction zone, be preferably methane in temperature required scope.Approximately from envrionment temperature to 1200 (650 ℃) and at the input fuel gas down of about 30～3500psig(0.03～24Mpa).Say that quantitatively carbon containing slurry, fuel gas and oxygen-containing gas are about 0.9～2.27 amount feed with the weight ratio of free oxygen and carbon.
The carbon containing slurry is through feeder sleeve, in the preferable flow rate inflow divider 16 with about 0.1～5 feet per second (0.03～1.5 meter per second).Because carbon containing slurry 25 diameters are less, so the flow velocity of carbon containing slurry is increased to the scope of about 1～50 feet per second (0.3～1.5 meter per second).
Oxygen-containing gas is generally worn footpath gas passage 27 through feeder sleeve 24 feed and be divided into two strands of air-flows, flows through passage 29 as another to form the truncated cone air-flows.The oxygen-containing gas air-flow can have various flow velocitys, and for example, the flow velocity by gas passage 27 can be 200 feet per seconds (8～60 meter per seconds), and can be 300 feet per seconds (90 meter per seconds) by the flow velocity of truncated cone passage 29.As noted above, annular carbon containing slurry stream in carbon containing slurry pipe 25 with pipe 28 and pipe 23 nethermost truncated cone oxygen flow intersections down.By truncated cone oxygen flow annular carbon containing slurry is produced shearing action, the carbon containing slurry that contains oxygen-containing gas is disperseed substantially from pipeline 27.
Then, the dispersion that obtains is by acceleration zone 33, and the selected cross section and the shape of acceleration zone 33 be, makes oxygen-containing gas accelerate to enough two-forties, further makes the carbon containing slurry be atomized into medium big small volume drops in about 100～600 micrometer ranges.
When burner noz(zle) 10 had just been started working, the reinforced rate of fuel device was compared with carbon containing slurry feed rate and is preponderated, but when the reinforced increase of carbon containing slurry, the reinforced rate of fuel gas then reduces.Thisly stop fully until fuel gas is reinforced from the reinforced reinforced process of carbon containing slurry that slowly is transformed into of fuel gas.In case reaction takes place to disturb and reinforced simultaneously must the minimizing, then fuel gas is with a certain amount of air feed again, so that make reaction zone remain on temperature required scope.
With reference now to Fig. 2 and Fig. 4,, can see another embodiment of the present invention, it is generally with numeral 110 expressions.Technology burner 110 has a pipe core 112, and this pipe core is by plate 114 sealings on its top.The upper end of pipe 112 is carbon containing slurry filling tubes 122.Pipe 112 is limited to inside with carbon containing slurry pipe 113, and the latter has a undergauge 116 at its foot.Because the foot diameter reduces gradually, the carbon containing slurry accelerates to about 1～50 feet per second (0.3～15 meter per second) because the pipe 112 above the undergauge district has than major diameter, therefore manages 112 and is seldom stopped up.
Pipe 124 is concentric with pipe 112, and internal diameter is greater than the external diameter of pipe 112.Managing 124 upper ends seals with ring-like plate 120.For the ring-like as shown in Figure 2 plate 120 of fixed tube 112 has an aperture.Oxygen-containing gas filling tube 114 is installed near pipe 124 tops.Lower end at pipe 124 has the frusto-conical surface 126 of contraction.This surface extends under the internal surface of determining undergauge 116, as shown in Figure 2.Frusto-conical surface 126 cooperates with frusto-conical surface 118, constitutes truncated cone pipe 127, as the passage of oxygen-containing gas.Distance is definite between the frusto-conical surface 118 and 126, is that the flow velocity that requires is determined when wearing footpath truncated cone pipe 127 by oxygen-containing gas.In general, for the flow velocity of discussing later, two butt cone surface spacings are greatly about 0.05～0.95 inch (in 0.13～2.4cm) scope.When oxygen-containing gas is worn footpath truncated cone pipe 127, desired flow velocity will influence the shearing action of the carbon containing slurry in the pipe 113.This shearing action makes the dispersion of the carbon containing slurry in the oxygen-containing gas very even.
The angle that frusto-conical surface is being prolonged in about 15 °～75 ° scopes converges at the longitudinal axis that pipe 112 prolongs.If angle is too little, as 10 °, oxygen-containing gas impact surface then, energy consumption is very big.But if angle is too big, then the shearing action of Huo Deing is very little again.
Acceleration zone 130 is about the summit of frusto-conical surface 126.Concerning Fig. 2 and embodiment illustrated in fig. 4, this acceleration zone is the cylinder of a full hole heart, and is porose 131 in cylinder upper end, in the cylinder lower end porose 133.With liquid flowing ratio, the size of acceleration zone 130 can be used for the identical of Fig. 1 and Fig. 3 embodiment acceleration zone 33, be preferably wear-resisting pipe be housed, the acceleration zone of the wear-resisting pipe that for example a kind of wolfram varbide is made.
Water jacket 146 is installed and with one heart from managing the outwards displacement of 124 outer walls footpath, and at the water jacket upper end closed, and plate 148 has a hole with ring-like plate 148, in order to wear directly and mounting pipe 124, as shown in Figure 2.Plate 148 also has other three holes, is used for wearing directly and installing of fuel gas filling tube 136 and 138.The filling tube that is connected with fuel gas pipe 143 is not shown.Water jacket 146 provides the ring-like space of being determined by the outer wall of pipe 124 and its inwall 145.In ring-like space 145, three fuel gas pipes 142,143 and 152 are arranged.These pipes are determined fuel gas passage 142a, 143a and 152a respectively.From Fig. 2 and Fig. 4 as seen, fuel gas pipe 142,143 and 152 has isogonism and identical spacing, and its angle is downwards towards the longitudinal axis extension direction of pipe 112.The indicated this angle of embodiment of Fig. 2 and spacing are identical with the angle of the Fig. 1 of previous embodiment and fuel gas pipe shown in Figure 3.
Fuel gas pipe is not only contained in ring-like space 145, and it also is used to provide latus rectum water coolant filling tube.The cooling-water duct pipe 150 of 150 inputs is positioned at the upper end of water jacket 146.Water jacket 146 has ring-like plate in its lower end, and the latter provides water channel 147, as shown in Figure 2.It may be noted that also fuel gas pipe passes the hole of flange 140 for for the purpose of installing.
The concentric outer burner wall 154 of technology burner 110 equipments, and have bottom surface 158.Heating wall 154 radially outward be shifted, provides water-cooled tube 151 so that manage 146 outer wall with its inwall.Water pipe 151 carries out liquid transfer by water channel 147 and annular space 145.Therefore, the water that enters in the filler pipe 150 is worn ring-like space 145, footpath, flows into water channel 147, upwards enters pipe 151 thus, so that can drain by water shoot 160.Water pipe 151 seals with annular flange dish 156 at its top.
With ring flange 162, the technology burner is fixed on the producer gas generator, so that technology burner 110 directly enters reaction zone with gas.The installation of technology burner 110 not only can be temporary transient but also can be permanent, and this depends on whether it replaces preheat burner or use jointly with the preheater of permanent installation.After reaction zone has risen to temperature required scope, when preheat burner will replace with technology burner 110, use temporarily and install, and preheat burner uses forever and installs when forever being installed in container.
In working order, reaction zone is finished pre-heating stage, make its temperature rise to about 1500～2500 °F (810～1370 ℃) after, technology burner 110 is inserted passages.After adding feed liquid and leaving the technology burner, about 1～10 second of its residence time in reactor.Oxygen-containing gas in technology burner 110 reinforced is the temperature range at about envrionment temperature to 1200 (650 ℃).And the reinforced of carbon containing slurry is to arrive in the temperature of saturation scope of carrier liq in about envrionment temperature.It is to carry out under the temperature of about envrionment temperature to 1200 (650) that fuel gas supplies in technology burner 110.For pressure, in burner, and the carbon containing slurry is reinforced under the pressure of about 30～3500psig(0.3～24Mpa) to oxygen-containing gas with the forced feed of about 30～3500psig(0.3～24Mpa).Usefully the pressure that fuel gas is added is about 30～3500psig(0.3～24Mpa).Carbon containing slurry, fuel gas and oxygen-containing gas with q.s in burner, with scope that free oxygen and carbon weight ratio are provided about 0.9～2.27.
When burner nozzle 110 had just been started working, the gas feed rate was greater than the carbon containing slurry.But because the fuel gas charging reduces, then the carbon containing slurry is reinforced increases.Until there not being fuel gas to add, the reinforced maximum rate that reaches of carbon containing slurry in case whole or local dry burning carbon containing slurry take place, also can be sent fuel gas into pipeline, to help to keep reaction zone temperature.
The carbon containing slurry is gone into together with about 0.1～5 feet per second (0.03～1.5 meter per second) speed.When carbon containing slurry process manages 113, it and the diameter shrinkage part intersection of managing 112.Whereby, the speed of carbon containing slurry is brought up in about 1～50 feet per second (0.3～15 meter second) scope, the carbon containing slurry in pipe 112 and with the intersection of the frustum of a cone liquid of oxygen-containing gas stream, this oxygen-containing gas provides by frustum of a cone pipe 127.The flow velocity of this frustum of a cone liquid stream arrives the velocity of sound at about 75 feet per seconds (23 meter per second).The shearing action that the carbon containing slurry is obtained makes its ten minutes homodisperse in oxygen-containing gas.Dispersion is mixed, and wears footpath acceleration zone 130 then, and this district 130 has the same cross section of pipe 113 and frustum of a cone pipe 127.Identical with the acceleration zone of the embodiment of aforesaid Fig. 1 and Fig. 3.The pressure of acceleration zone 130 in hole, its underpart 133 is lower than its upper hole 131.This pressure reduction quickens oxygen-containing gas, so that because the dispersion batch mixing is worn the footpath acceleration zone, make dispersed carbon containing slurry produce atomizing.The atomizing particle that obtains is in about 100～600 microns.
When feed gas is added the technology burner, its stimulate the menstrual flow fuel gas filling tube 136,138 and similar pipe that does not illustrate.

Claims (12)

1, a kind of processing contains H 2Method with CO gas, this method is a part oxidizing carbonaceous slurry in a container, this container have maintain usually about 15～3500pig (reaction zone under the pressure in 0.2～24MPa) scope and about 1700～3500 (930～1930 ℃) temperature, its improvements comprise:
(a), a kind of carbon containing slurry and a kind of oxygen-containing gas are introduced described reaction zone, described carbon containing slurry homodisperse and enter reaction zone at described reactant and atomized in the past substantially in described oxygen-containing gas as reactant;
(b) fuel gas of requirement is introduced described reaction zone to keep described reaction zone in described temperature, after described fuel enters described reaction zone, directly described fuel gas is introduced the reactant of (a), the reactant that mixes described fuel gas and enter;
(c) by part oxygen, the reactant (a) that makes introduction prepares the described H that contains at described reaction zone internal reaction 2With the gas of CO, and;
(d), make the fuel gas (b) of the introducing of described amount and oxygen-containing gas reactant (a) reaction of at least a portion introduction by partial oxidation.
2, method according to claim 1, wherein the described dispersion of the uniform carbon containing slurry of described cardinal principle in described oxygen-containing gas is so implemented: the frustum of a cone body fluid stream of a described oxygen-containing gas is provided and provides a cylinder body fluid flow simultaneously with second speed with first rate, the described circular cone body fluid flow of described carbon containing slurry is with the internal surface phase intersection of the angle in about 15 °～75 ° scopes at the described frustum of a cone body fluid stream of described oxygen-containing gas, wherein said first rate is in about 75 feet per seconds (23 meter per second) arrive the scope of the velocity of sound, and described second speed is in about 1～50 feet per second (0.3～15 meter per second) scope.
3, method according to claim 1, the dispersion of the uniform described carbon containing slurry of wherein said cardinal principle and described oxygenous be to implement by following 3 sections:
(1) the cylinder body fluid flow of described oxygen-containing gas has first rate;
(2) the annular liquid stream of described carbon containing slurry has second speed; And
(3) the frustum of a cone body fluid stream of described oxygen-containing gas has third speed;
Described liquid stream essentially concentric and radially discharge, so that described cylinder body fluid flow is in described annular liquid stream and the internal surface intersection of flowing with angle in about 15 °～75 ° scopes and described frustum of a cone body fluid of annular liquid stream, wherein said second speed in about 1～5 feet per second (0.3～15 meter per second) scope and described first and third speed in about 75 feet per seconds (23 meter per second) arrive velocity of sound scope.
4, according to claim 1,2 or 3 described methods, the atomizing of wherein said carbon containing slurry is by the described basic thing that disperses is uniformly worn zone that basic dispersion reactant is uniformly quickened, footpath, atomize by this, described oxygen-containing gas composition quickens with the speed greater than the carbon containing slurry composition of described basic homogeneous dispersion.
5, method according to claim 4 wherein by described zone is applied a pressure reduction, is finished described acceleration.
6, according to claim 2 or 3 described methods, wherein said fuel gas is introduced described reaction zone with two strands of liquid streams at least.
7, according to the described method of claim 1, wherein pressure is the scope at about 150～2500psig(10.4～17.3MPa).
8, burner, it comprises:
(a) hollow cylinder pipe core has the liquid feeding device and has a feed port in its most proximal end in its distal-most end;
(b) first ring pipe, coaxial and external with the described center of a part pipe range at least, described first ring pipe has the liquid feeding device and in its most proximal end one feed port is arranged in its distal-most end;
(c) second ring pipe, coaxial and external with at least a portion described first annular pipe range, and described second ring pipe has liquid feeding device and in distal-most end one hole is arranged in its distal-most end;
(d) hollow cylinder acceleration tube, its cross section be less than the adduction in described pipe core, described first ring pipe and three cross sections of described second ring pipe, and in its most proximal end, in the outside of described burner one feed port is arranged;
(e) frusto-conical surface tube stub is the distal-most end of described acceleration tube on its summit, is the most proximal end external diameter of described second ring pipe in its bottom surface;
(f) at least one flue, it carries out liquid transfer with the mouth of pipe that is positioned on the outside of described burner.
9, burner, it comprises;
(a) hollow cylinder pipe core has feeding device in its distal-most end, in its most proximal end one hole is arranged;
(b) first ring pipe, coaxial and external with the described pipe core major axis of a part at least, the described first ring pipe distal-most end has a feed port;
(c) hollow cylinder acceleration tube, its cross section adds and the cross section less than described pipe core and described first ring pipe, and a feed port that is positioned at described burner outside is being arranged near end;
(d) frusto-conical surface tube stub is the distal-most end of described acceleration on its summit, is the described first ring pipe distal-most end external diameter in its bottom surface, and
(e) at least one flue, it can carry out the fluid transmission with the pipe that is positioned on the described burner outside.
10, according to Claim 8 or 9 described burners, wherein have at least two described mouths of pipe to shift out with being equal to and the described hole of isogonism ground on being positioned at outside the described burner around.
11, burner according to claim 9, the plane of the most proximal end of wherein said pipe core between residing plane, described truncated cone bottom surface and the described plane, summit of described frustum of a cone.
12, burner according to claim 8, the plane of the most proximal end of wherein said first ring pipe between residing plane, described truncated cone bottom surface and the residing plane, summit of described truncated cone.
CN86102626A 1985-04-16 1986-04-16 Process and apparatus for use with pressurized reactors Expired CN1010027B (en)

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US723,771 1985-04-16

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CN102086415A (en) * 2009-12-03 2011-06-08 通用电气公司 Feeding device and feeding method
CN104560213A (en) * 2013-10-22 2015-04-29 任相坤 Coal-water slurry and natural gas joint gasifying nozzle
CN109876727A (en) * 2019-02-21 2019-06-14 亚泰半导体设备股份有限公司 High mixture ratio mixing device and the preparation production system for using it
CN111349470A (en) * 2018-12-24 2020-06-30 国家能源投资集团有限责任公司 Burner and gasification furnace with same

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DE4416037C1 (en) * 1994-05-06 1995-09-07 Noell Dbi Energie Entsorgung Pressurised gasification reactor sealed by disc fabricated by conjoined pipe rings
EP0652276A1 (en) * 1994-05-11 1995-05-10 Norsk Hydro A/S Method for combustion of combustible material
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US9328301B2 (en) 2009-12-03 2016-05-03 General Electric Company Injector and method for co-feeding solid and liquid fuels
CN104560213A (en) * 2013-10-22 2015-04-29 任相坤 Coal-water slurry and natural gas joint gasifying nozzle
CN111349470A (en) * 2018-12-24 2020-06-30 国家能源投资集团有限责任公司 Burner and gasification furnace with same
CN111349470B (en) * 2018-12-24 2021-04-13 国家能源投资集团有限责任公司 Burner and gasification furnace with same
CN109876727A (en) * 2019-02-21 2019-06-14 亚泰半导体设备股份有限公司 High mixture ratio mixing device and the preparation production system for using it
CN109876727B (en) * 2019-02-21 2021-05-04 亚泰半导体设备股份有限公司 High ratio compounding device and use its preparation production system

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AU5051290A (en) 1990-08-16
ZA862850B (en) 1987-12-30
DE3669733D1 (en) 1990-04-26
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EP0205238B1 (en) 1990-03-21
KR860008258A (en) 1986-11-14
EP0205238A3 (en) 1987-05-06
KR930011070B1 (en) 1993-11-20
IN167311B (en) 1990-10-06
NZ215764A (en) 1989-04-26
TR22483A (en) 1987-08-10
CA1293125C (en) 1991-12-17
CN1010027B (en) 1990-10-17
AU596795B2 (en) 1990-05-17
AU5606986A (en) 1986-10-23

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