CN104178227A - Fluidized bed destructive distillation method and device of pulverized coal - Google Patents
Fluidized bed destructive distillation method and device of pulverized coal Download PDFInfo
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- CN104178227A CN104178227A CN201310210239.7A CN201310210239A CN104178227A CN 104178227 A CN104178227 A CN 104178227A CN 201310210239 A CN201310210239 A CN 201310210239A CN 104178227 A CN104178227 A CN 104178227A
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Abstract
The invention discloses a fluidized bed destructive distillation method and device of pulverized coal. The destructive distillation method comprises the following steps: A. preheating a pulverized coal feedstock in a pulverized coal feedstock preheating tube (12) by absorbing heat generated by combustion reactions in a gasification burner (11); B. subjecting the preheated pulverized coal feedstock to a destructive distillation reaction in a bed-layer-type fluidized bed destructive distillation reactor (9) for generation of oil gas and pulverized coal semicoke, and stripping oil gas entrained in the pulverized coal semicoke in a steam stripping device (18); C. introducing the pulverized coal semicoke after stripping into the gasification burner for combustion reaction with oxygen; D. subjecting pulverized coal semicoke after partial combustion in the step C and water steam to a water gas reaction in a riser gasification reactor (2); and E. introducing gas and high temperature ash generated in the step D into an ash gas separator (1) for gas-solid separation. The invention discloses a fluidized bed destructive distillation device of pulverized coal for realizing the above method. The invention can be used for destructive distillation processing of a variety of pulverized coals.
Description
Technical field
The invention belongs to coal dust retorting technique field, relate to a kind of fluidized bed dry distillation method and device of coal dust.
Background technology
The crude oil demand of China's rapid growth has pulled the rapid growth of crude oil import amount, and externally interdependency improves constantly, and the energy security guarantee of China has been brought to very large hidden danger.The shortage of hydrocarbon resources and demand promote, and make the cost of a lot of petrochemical materialss also high.Coal Chemical Industry and petrochemical complex have mutually substituting, and Development of Novel Coal Chemical Industry can be used as petrochemical complex and well supplements, necessary.Coal Chemical Industry refers to taking coal as raw material, makes coal be converted into the process of gas, liquid and solid fuel and chemical through chemical process; Mainly comprise coal gasification, liquefaction, destructive distillation, and tar processing and carbide acetylene chemical industry etc.
Dry distillation of coal technology is one of significant process of Coal Chemical Industry.Coal low-temperature pyrolysis can be extracted semi coking tar, and produces semicoke and coalitenessity producer gas.Tar yield is higher, and composition, taking alkane as main, can further process senior liquid fuel (the such as vehicle fuel such as gasoline, diesel oil) and industrial chemicals; Semicoke can be used as solid fuel or gasified raw material, and coal gas is good fuel and chemosynthesis raw material.Dry distillation of coal technology can be divided into moving-bed destructive distillation, fluidized bed dry distillation etc.Wherein the fluidized bed dry distillation of coal dust is to be fine powder (particle diameter≤3mm) by block coal pulverizer, the process of the concurrent heat-dissipating decomposition reaction of direct contact heat transfer under fluidized state with high-temp solid thermal barrier (coal ash) or high-temperature gas thermal barrier; Have that hot strength is high, dry distillation rate is fast, the oil gas residence time is short, gas-solid can sharp separation etc. feature, be a kind of coal processing and utilization mode preferably.
Chinese patent CN101328415A discloses a kind of piston type fluidized bed low temperature dry distillation technological process, can be for the destructive distillation of coal dust.This processing method is utilized lifting tube flowing catalytic cracking device principle, taking riser reactor as dry distillation reactor device, and taking catalyst regenerator as high-temperature water gas producer, fluidizing medium and thermal barrier taking high-temperature water gas as destructive distillation raw material.Destructive distillation raw material is transported in riser tube fluidized-bed reactor and carries out dry distillation reactor, and after reaction, oil gas separates and obtains destructive distillation product.Pyrolysis Char enters water-gas machine, and carbon, the airborne oxygen in Pyrolysis Char and water vapor is oxidized and water-gas reaction obtains water-gas.This processing method mainly has the following disadvantages: (1) adopts fluidizing medium and the thermal barrier of high-temperature water gas (approximately 620～900 DEG C) as retort process, need to high-temperature water gas be transported to riser tube dry distillation reactor device from water-gas machine with gas compressor.Carry high-temperature water gas to propose higher material requirement to gas compressor; Gas compressor, all the time in the harsh running condition of height, will have influence on the long-term operation of destructive distillation device in addition.(2) pressurized air and water vapor enter the bottom of high-temperature water gas producer simultaneously, carry out combustion reactions and water-gas reaction at the same area and Pyrolysis Char simultaneously, cause between two kinds of reactions and influence each other; Burning and water-gas reaction can not fully be carried out, and can cause the productive rate reduction that generates water-gas from Pyrolysis Char.
Summary of the invention
The object of this invention is to provide a kind of fluidized bed dry distillation method and device of coal dust, carry required high temperature fluidized medium and gaseous heat-carrier, combustion reactions and the water-gas reaction of retort process to carry out and interactional problem at the same area to solve the existing gas compressor that need to use of existing powder fluidized bed retorting technique simultaneously.
For addressing the above problem, the technical solution used in the present invention is: a kind of fluidized bed dry distillation method of coal dust, is characterized in that: the method in turn includes the following steps:
A. the coal dust raw material after pulverizing enters the bottom of coal dust raw material preheating pipe through coal dust material feeding tube, up along coal dust raw material preheating pipe under the effect of the lift gas being passed into by lift gas jet pipe, the heat that coal dust semicoke after absorption stripping carries out combustion reactions generation in gasification combustor carries out preheating, and the coal dust raw material after preheating enters bed formula fluidized bed dry distillation reactor through coal dust raw material riser tube;
B. in the close phase section of the destructive distillation bed of coal dust raw material in bed formula fluidized bed dry distillation reactor, carry out dry distillation reactor, generate oil gas and coal dust semicoke, the first group cyclonic separator of oil gas in being located at bed formula fluidized bed dry distillation reactor isolated the defocused oil gas vent pipe by bed formula fluidized bed dry distillation reactor head of coal dust half and flowed out, coal dust semicoke in the close phase section of destructive distillation bed flows downward, enter the stripper of being located at bed formula fluidized bed dry distillation reactor below, in stripper, pass into water stripping steam, stripping goes out coal dust semicoke entrained oil gas;
C. in stripper, the coal dust semicoke after stripping enters gasification combustor through coal dust semicoke transfer lime, carry out combustion reactions with the oxygen passing in gasification combustor through combustion gases sparger, the carbon monoxide, carbonic acid gas generating after burning carrying together with atomized water steam that pass through partially combusted coal dust semicoke upwards mobile, enters riser tube gasifying reactor;
D. in riser tube gasifying reactor, enter the partially combusted coal dust semicoke of process in riser tube gasifying reactor and atomized water steam and pass into gasified water steam in riser tube gasifying reactor along the up water-gas reaction of carrying out of riser tube gasifying reactor, the coal gas of generation and high temperature coal ash enter coal ash coal gas separator;
E. in coal ash coal gas separator, coal gas and high temperature coal ash carry out gas solid separation in second group of cyclonic separator, and isolated coal gas is flowed out by the gas outlet tube at coal ash coal gas separator top.
Be used for the fluidized bed dry distillation device of the coal dust of realizing above-mentioned method for destructive distillation, be provided with fluidized bed dry distillation reactor, Pyrolysis Char burning and gasifying reactor, fluidized bed dry distillation reactor is provided with coal dust material feeding tube, it is characterized in that: dry distillation reactor device is bed formula fluidized bed dry distillation reactor, in it, be provided with first group of cyclonic separator, top is provided with oil gas collection chamber, oil gas vent pipe, below is coaxially arranged with stripper with it, in stripper, be provided with stripping baffles, bottom is provided with stripped vapor sparger, Pyrolysis Char burning comprises gasification combustor and riser tube gasifying reactor with gasifying reactor, gasification combustor is positioned at the below of riser tube gasifying reactor, the housing of gasification combustor comprises the cylindrical drum of bottom and the round table surface shape cylindrical shell on top, between the side of cylindrical drum and the bottom bulkhead of stripper, be provided with coal dust semicoke transfer lime, in gasification combustor, be coaxially arranged with coal dust raw material preheating pipe with it, the bottom of coal dust raw material preheating pipe is stretched out by the bottom of gasification combustor, described coal dust material feeding tube is located at the bottom of coal dust raw material preheating pipe, the bottom of coal dust raw material preheating pipe is provided with lift gas jet pipe, the top exit of coal dust raw material preheating pipe is connected with pipe connecting, pipe connecting is stretched out by gasification combustor, its top exit is connected with the bottom inlet of coal dust raw material riser tube, the top exit of coal dust raw material riser tube is connected with horizontal pipeline section, the outlet of horizontal pipeline section is positioned at the dilute phase section of bed formula fluidized bed dry distillation reactor, the bottom of gasification combustor is provided with combustion gases sparger, combustion gases sparger is connected with inlet pipe, inlet pipe is with oxygen intake and atomized water steam-in, riser tube gasifying reactor is the rounded vertical tube of cross section, its bottom inlet is connected with the top exit of gasification combustor, bottom is provided with gasified water steam inlet tube, the top of bed formula fluidized bed dry distillation reactor is provided with coal ash coal gas separator, in it, be provided with second group of cyclonic separator, the top exit of riser tube gasifying reactor is connected with second group of cyclonic separator by one section of level pipe, the top of coal ash coal gas separator is provided with coal gas collection chamber, gas outlet tube, bottom is provided with fluidizing agent sparger.
Adopt the present invention, there is following beneficial effect: (1) retort process of the present invention is used bed formula fluidized bed dry distillation reactor, coal dust raw material absorbs the heat that coal dust semicoke after stripping carries out combustion reactions generation in gasification combustor and carries out preheating in coal dust raw material preheating pipe, and does not use gaseous heat-carrier.Oil gas and water vapor that the destructive distillation of coal dust raw material generates, and the oil gas that the defocused water stripping steam of stripping coal dust half and stripping go out in stripper, can make the close phase section of destructive distillation bed in bed formula fluidized bed dry distillation reactor in inflation fluidized state, so do not need to provide specially fluidizing medium.In a word, the present invention does not need to use gas compressor to carry high temperature fluidized medium and thermal barrier for retort process, does not exist to gas compressor is proposed the problem of higher material requirement and makes gas compressor have influence on all the time the problem of destructive distillation device long-term operation in the harsh running condition of height.The present invention does not use high-temp solid thermal barrier heating coal dust raw material yet, thereby can improve the treatment capacity of destructive distillation device coal dust raw material.(2) the present invention, combustion reactions is carried out in gasification combustor, water-gas reaction is carried out in riser tube gasifying reactor, two kinds of reactions separately independently region carry out, between do not influence each other.Combustion reactions can be water-gas reaction enough heats is provided; In riser tube gasifying reactor, water-gas reaction can fully be carried out, and is conducive to improve the productive rate that generates water-gas from coal dust semicoke.(3) the present invention, through destructive distillation and water-gas reaction, coal dust raw material can be fully used; The last solid product generating of coal dust raw material is coal ash, thereby can reduce the reserve of coal ash coal gas separator, makes its scantlings of the structure less, reduces investment outlay.
The present invention can be used for the destructive distillation processing of multiple coal dust, and the course of processing can be continuously, stably carry out, and flexible adjustment, treatment capacity are large, and the yield of oil gas and coal gas is high.
Below in conjunction with the drawings and specific embodiments, the present invention is further detailed explanation.The drawings and specific embodiments do not limit the scope of protection of present invention.
Brief description of the drawings
Fig. 1 is the schematic diagram of powder fluidized bed destructive distillation device of the present invention.
Embodiment
Referring to Fig. 1, powder fluidized bed destructive distillation device of the present invention (referred to as destructive distillation device) is provided with fluidized bed dry distillation reactor, Pyrolysis Char burning and gasifying reactor, and fluidized bed dry distillation reactor is provided with coal dust material feeding tube 15.Dry distillation reactor device is bed formula fluidized bed dry distillation reactor 9, and the housing of bed formula fluidized bed dry distillation reactor 9 comprises the cylindrical drum of upper and lower and the inverted round table face shape cylindrical shell between these two cylindrical shells.In bed formula fluidized bed dry distillation reactor 9, be provided with first group of cyclonic separator 8, comprise the cyclonic separator of two series connection, its dipleg stretches to the top within the close phase section of destructive distillation bed.The top of bed formula fluidized bed dry distillation reactor 9 is provided with oil gas collection chamber 6, oil gas vent pipe 7, and below is coaxially arranged with stripper 18 with it.The housing of stripper 18 comprises a cylindrical drum; In stripper 18, be provided with stripping baffles (shown in Fig. 1 is herring-bone stripping baffles), bottom is provided with stripped vapor sparger 17.
Pyrolysis Char burning of the present invention comprises gasification combustor 11 and riser tube gasifying reactor 2 with gasifying reactor, and gasification combustor 11 is positioned at the below of riser tube gasifying reactor 2.The housing of gasification combustor 11 comprises the cylindrical drum of bottom and the round table surface shape cylindrical shell on top, between the side of cylindrical drum and the bottom bulkhead of stripper 18, is provided with coal dust semicoke transfer lime 16.Coal dust semicoke transfer lime 16 is provided with flowrate control valve 23, with the flow of coal dust semicoke in control tube.
In gasification combustor 11, be coaxially arranged with coal dust raw material preheating pipe 12 (main part of coal dust raw material preheating pipe 12 is located in gasification combustor 11) with it, between the cylindrical drum of gasification combustor 11 and coal dust raw material preheating pipe 12, form circular channel 27 (shape of cross section is annular).The bottom of coal dust raw material preheating pipe 12 is stretched out by the bottom of gasification combustor 11; Described coal dust material feeding tube 15 is located at the bottom of coal dust raw material preheating pipe 12, and the bottom of coal dust raw material preheating pipe 12 is provided with lift gas jet pipe 14.The top exit of coal dust raw material preheating pipe 12 is connected with pipe connecting 20; Pipe connecting 20 is stretched out by gasification combustor 11, and its top exit is connected with the bottom inlet of coal dust raw material riser tube 10.The top exit of coal dust raw material riser tube 10 is connected with horizontal pipeline section 101, and the outlet 102 of horizontal pipeline section 101 is positioned at the dilute phase section of bed formula fluidized bed dry distillation reactor 9.The bottom of gasification combustor 11 is provided with combustion gases sparger 13 around coal dust raw material preheating pipe 12; Combustion gases sparger 13 is connected with inlet pipe 131, and inlet pipe 131 is with oxygen intake and atomized water steam-in.
Coal dust raw material preheating pipe 12, coal dust raw material riser tube 10 and riser tube gasifying reactor 2 are the rounded vertical tube of cross section.The bottom inlet of riser tube gasifying reactor 2 is connected with the top exit of gasification combustor 11, and bottom is provided with gasified water steam inlet tube 201.Gasified water steam inlet tube 201 is tilted to, and normally evenly arranges 2～6 around riser tube gasifying reactor 2.The vertical range b of center to the junction of riser tube gasifying reactor 2 bottom inlets and gasification combustor 11 top exits of gasified water steam inlet tube 201 and riser tube gasifying reactor 2 interfaces, is generally 0.5～1m (rice).
The top of bed formula fluidized bed dry distillation reactor 9 is provided with coal ash coal gas separator 1, and the housing of coal ash coal gas separator 1 comprises the cylindrical drum of upper and lower and the inverted round table face shape cylindrical shell between these two cylindrical shells.In coal ash coal gas separator 1, be provided with second group of cyclonic separator 24, comprise the cyclonic separator of two series connection, its dipleg stretches to the top within coal ash dense-phase bed; The top exit of riser tube gasifying reactor 2 is connected with second group of cyclonic separator 24 by one section of level pipe 203.The top of coal ash coal gas separator 1 is provided with coal gas collection chamber 25, gas outlet tube 26, and bottom is provided with fluidizing agent sparger 4.
Coal ash coal gas separator 1 is provided with external warmer 22, between external warmer 22 and the lower cylindrical cylindrical shell of coal ash coal gas separator 1, is provided with cement output tank 221 and return tube 222.Cement output tank 221 is provided with flowrate control valve 23, with the flow of coal ash in control tube.External warmer 22 is also connected with coal ash tank 21 by pipeline 223, and coal ash tank 21 is a metal vessel.The heat-obtaining medium of external warmer 22 typically uses the water under envrionment temperature.
Referring to Fig. 1, the height a of gasification combustor 11 is generally 2～10m, and the diameter of cylindrical drum is generally 1000～5000mm.The height h of riser tube gasifying reactor 2 is generally 10～40m, and riser tube gasifying reactor 2 is generally 20%～50% of gasification combustor 11 cylindrical drum cross-sectional areas with the cross-sectional area of coal dust raw material preheating pipe 12.Above-mentioned cross-sectional area, the diameter of pressing respectively riser tube gasifying reactor 2, coal dust raw material preheating pipe 12 and gasification combustor 11 cylindrical drums calculates.
The various device of destructive distillation device of the present invention, pipeline, member, all adopt metallic substance manufacture.The inner walls of bed formula fluidized bed dry distillation reactor 9, stripper 18, gasification combustor 11, coal ash coal gas separator 1 etc., the inwall of riser tube gasifying reactor 2, coal dust raw material riser tube 10 and other pipeline contacting with solid particulate (coal dust semicoke, coal ash etc.), can arrange heat insulation and wear resistance layer (figure slightly) as required.Coal dust raw material preheating pipe 12 does not arrange heat insulation and wear resistance layer, but therein, outer wall all arranges heat conduction wearing layer (material is silicon carbide, corundum etc., figure slightly).The shape of cross section of various pipelines is circle.The diameter that the present invention mentions, is the interior diameter of cylindrical shell or pipeline; The coal dust raw material preheating pipe 12 that is provided with the cylindrical shell of heat insulation and wear resistance layer or pipeline and inwall and is provided with heat conduction wearing layer for inwall, diameter is the interior diameter of heat insulation and wear resistance layer or heat conduction wearing layer.The diameter of each pipeline is mainly determined according to the flow of material and/or medium in each pipeline, density calculation.
Stripped vapor sparger 17, fluidizing agent sparger 4, combustion gases sparger 13 can use conventional annular sparger or dendroid sparger.Flowrate control valve can use the flowrate control valve (as guiding valve) of various conventional control granular solid particle flows.External warmer 22, cyclonic separator etc. can use this area or near field to commonly use.
The method (referred to as method for destructive distillation) that adopts the destructive distillation device shown in Fig. 1 to carry out powder fluidized bed of the present invention destructive distillation, in turn includes the following steps:
A. the coal dust raw material 150 after pulverizing enters the bottom of coal dust raw material preheating pipe 12 through coal dust material feeding tube 15, up along coal dust raw material preheating pipe 12 under the effect of the lift gas 140 being passed into by lift gas jet pipe 14, a part of heat that the coal dust semicoke after absorption stripping carries out combustion reactions generation in gasification combustor 11 carries out preheating.Coal dust raw material 150 (together with lift gas 140) after preheating is through pipe connecting 20, coal dust raw material riser tube 10, horizontal pipeline section 101, entered the dilute phase section of bed formula fluidized bed dry distillation reactor 9 by the outlet 102 of horizontal pipeline section 101, to falling in the close phase section of destructive distillation bed.In Fig. 1, Reference numeral 19 represents the interface of the close phase section of destructive distillation bed; The below at this interface is the close phase section of destructive distillation bed, and top is the dilute phase section of bed formula fluidized bed dry distillation reactor 9.
B. in the close phase section of the destructive distillation bed of coal dust raw material 150 in bed formula fluidized bed dry distillation reactor 9, carry out dry distillation reactor, generate coal tar oil gas (referred to as oil gas) and coal dust semicoke.Oil gas upwards flows into the dilute phase section of bed formula fluidized bed dry distillation reactor 9, together with the lift gas 140 that enters this dilute phase section, after isolating coal dust semicoke, first group of cyclonic separator 8 in being located at bed formula fluidized bed dry distillation reactor 9 enter the oil gas collection chamber 6 at bed formula fluidized bed dry distillation reactor 9 tops, flowed out by the oil gas vent pipe 7 at bed formula fluidized bed dry distillation reactor 9 tops again, enter condensate recovery system.First group of isolated coal dust semicoke of cyclonic separator 8 through dipleg to falling in the close phase section of destructive distillation bed.
Coal dust semicoke in the close phase section of destructive distillation bed flows downward, and enters the stripper 18 of being located at bed formula fluidized bed dry distillation reactor 9 belows.In stripper 18, pass into water stripping steam 170 through stripped vapor sparger 17, stripping goes out coal dust semicoke entrained oil gas.Water stripping steam 170 after oil gas and stripping that stripping goes out upwards flows into bed formula fluidized bed dry distillation reactor 9, and the close phase section of the destructive distillation of flowing through bed enters the dilute phase section of bed formula fluidized bed dry distillation reactor 9; After first group of cyclonic separator 8 carries out gas solid separation, enter oil gas collection chamber 6, then flowed out by oil gas vent pipe 7.
C. the coal dust semicoke after the interior stripping of stripper 18 enters gasification combustor 11 (entering in circular channel 27) through coal dust semicoke transfer lime 16.Oxygen intake in inlet pipe 131 and atomized water steam-in pass into oxygen 132 and atomized water steam 133 respectively in combustion gases sparger 13, make both after the interior mixing of combustion gases sparger 13, spray, enter circular channel 27.In circular channel 27, the coal dust semicoke after above-mentioned stripping contacts with the mixture of atomized water steam 133 with oxygen 132, carries out combustion reactions with oxygen 132; The carbon monoxide, carbonic acid gas generating after burning carrying together with atomized water steam 133 that pass through partially combusted coal dust semicoke upwards mobile, enters the riser tube gasifying reactor 2 of being located at gasification combustor 11 tops.The main heat carrier that heat is provided to the water-gas reaction of following step D through partially combusted coal dust semicoke (be charcoal only some participates in combustion reactions) in the coal dust semicoke after stripping.Atomized water steam 133 is mainly to make the coal dust semicoke after stripping reach atomizing state, thereby makes coal dust semicoke mix fully, to burn with oxygen 132.
Above-mentioned combustion reactions is mainly charcoal in the coal dust semicoke after stripping and the reacting of oxygen 132.The gaseous product that burning generates is mainly carbon monoxide and carbonic acid gas.Coal dust semicoke after stripping carries out in the process of combustion reactions in gasification combustor 11, the coal dust raw material 150 of the heat that heat self-contained a part and combustion gas are carried in the tube wall of coal dust raw material preheating pipe 12 passes to coal dust raw material preheating pipe 12, carries out preheating to coal dust raw material 150.
D. in riser tube gasifying reactor 2, enter the partially combusted coal dust semicoke of process in riser tube gasifying reactor 2 and atomized water steam 133 and through gasified water steam inlet tube 201 pass into gasified water steam 202 in riser tube gasifying reactor 2 with piston flow form along the up water-gas reaction of carrying out of riser tube gasifying reactor 2.Coal gas (main component is carbon monoxide and hydrogen) and high temperature coal ash that water-gas reaction generates enter coal ash coal gas separator 1 through level pipe 203.A small amount of remaining water vapor (comprising atomized water steam 133 and gasification water vapor 202) and enter the carbon monoxide that the step C combustion reactions in riser tube gasifying reactor 2 generates and together enter coal ash coal gas separator 1 thereupon.The carbon monoxide that step C combustion reactions generates also counts in the coal gas that water-gas reaction generates.
Above-mentioned water-gas reaction is thermo-negative reaction, principal reaction have coal dust semicoke after stripping gasification combustor 11 interior after partial combustion remaining charcoal react and generates carbon monoxide and hydrogen with water vapor (comprising atomized water steam 133 and gasification water vapor 202), also have the carbon dioxide reaction generation carbon monoxide in riser tube gasifying reactor 2 that enters of this remaining charcoal and step C combustion reactions generation.After water-gas reaction, described coal dust semicoke becomes high temperature coal ash (its carbon content is lower than 0.05%).
E. in coal ash coal gas separator 1, coal gas and high temperature coal ash (also having a small amount of remaining water vapor) carry out gas solid separation in second group of cyclonic separator 24.Isolated coal gas (also having a small amount of remaining water vapor) enters the coal gas collection chamber 25 at coal ash coal gas separator 1 top, then is flowed out by the gas outlet tube 26 at coal ash coal gas separator 1 top, enters gas recovery system; Isolated high temperature coal ash through dipleg to falling in coal ash dense-phase bed.Pass into fluidizing agent 5 (the normally water vapor of 450～550 DEG C) to the bottom of coal ash coal gas separator 1 through fluidizing agent sparger 4, the fluidizing agent 5 coal ash dense-phase bed of upwards flowing through, makes coal ash dense-phase bed in inflation fluidized state; The residual gas stripping that fluidizing agent 5 also can be carried the coal ash in coal ash dense-phase bed secretly simultaneously out.The residual gas that coal ash in the coal ash dense-phase bed that fluidizing agent 5 goes out together with stripping is carried secretly finally upwards flows into the dilute phase section of coal ash coal gas separator 1, after carrying out gas solid separation in the entrance on second group of cyclonic separator 24 enters second group of cyclonic separator 24, enter coal gas collection chamber 25, then flowed out by gas outlet tube 26.In Fig. 1, Reference numeral 3 represents the interface of coal ash dense-phase bed; The below at this interface is coal ash dense-phase bed, and top is the dilute phase section of coal ash coal gas separator 1.
Above-mentioned steps A～E continuously, loop; Main operational condition is generally as follows:
In steps A, the temperature of coal dust raw material 150 after the 12 interior preheatings of coal dust raw material preheating pipe is 450～550 DEG C; This temperature is measured at outlet 102 places of horizontal pipeline section 101.The residence time (carry out the time of preheating) of coal dust raw material 150 in coal dust raw material preheating pipe 12 be 0.5～3min (minute).Horizontal pipeline section 101 exports the pressure at 102 places, should be a little more than the working pressure at bed formula fluidized bed dry distillation reactor 9 tops.
The coal dust raw material 150 that the present invention can process can be brown coal, long-flame coal, bottle coal, non-caking coal or weakly caking coal etc.; Its particle diameter is not more than 3mm, and oleaginousness is 6%～25%, and water content is not higher than 20%.Particle diameter is measured with method of sieving, water content and Ge Jinfa (the lattice gold low-temperature pyrolysis test method of GB/T1341-2007 coal) mensuration for oleaginousness.
Steps A lift gas 140 used can be dry gas (main ingredient is methane), is to compress by the dry gas under envrionment temperature the compression dry gas forming, and pressure is 0.15～0.6MPa (pressure that the present invention mentions is gauge pressure).Lift gas 140 can also be water vapor, and temperature is 200～400 DEG C.
In step B, the dry distillation reactor time of coal dust raw material 150 in the close phase section of destructive distillation bed is 2～10min, the temperature (being dry distillation reactor temperature) of the close phase section of destructive distillation bed is 450～550 DEG C, the working pressure at bed formula fluidized bed dry distillation reactor 9 tops is 0.1～0.4MPa, and the linear gas velocity of bed formula fluidized bed dry distillation reactor 9 dilute phase sections is 0.2～1.2m/s (meter per second).The temperature of the close phase section of destructive distillation bed, refers to the medial temperature of the close phase section of destructive distillation bed.Gas in described linear gas velocity, is mainly oil gas and the water vapor that the destructive distillation of coal dust raw material generates, and the oil gas going out at the defocused water stripping steam 170 of the interior stripping coal dust half of stripper 18 and stripping.
Preferably 3～6min of dry distillation reactor time, preferably 470～530 DEG C of the temperature of the close phase section of destructive distillation bed.The dry distillation reactor time is preferably 3.5～4.5min, and the temperature of the close phase section of destructive distillation bed is preferably 490～510 DEG C.
The diameter of bed formula fluidized bed dry distillation reactor 9 top cylinder shape cylindrical shells is mainly according to the mobility scale calculative determination of bed formula fluidized bed dry distillation reactor 9 dilute phase section linear gas velocities, the height of the close phase section of destructive distillation bed is the reserve calculative determination of the dry distillation reactor time in the close phase section of destructive distillation bed and bed formula fluidized bed dry distillation reactor 9 interior coal dust semicokes according to coal dust raw material 150 mainly, and the height of bed formula fluidized bed dry distillation reactor 9 dilute phase sections is mainly according to the settling height calculative determination of coal dust semicoke.
In stripper 18, stripping temperature is 450～550 DEG C; This temperature is the medial temperature of the interior coal dust semicoke of stripper 18 bed.The coal dust semicoke entering in stripper 18 is gone out entrained oil gas by stripping after stripping; The coal dust semicoke that is gone out to carry secretly oil gas by stripping, its carbon content is generally 65%～85%.The percentage ratio that the present invention mentions, is weight percentage.
In step C, the temperature that passes into the atomized water steam 133 in combustion gases sparger 13 is 450～550 DEG C, and the temperature of oxygen 132 is 100～400 DEG C.The time that coal dust semicoke burns in gasification combustor 11 is 3～5min, and temperature of combustion is 800～900 DEG C (top at gasification combustor 11 is measured), and the working pressure at gasification combustor 11 tops is 0.15～0.5MPa.Should control the flow of oxygen 132, make the coal dust semicoke after stripping only carry out partial combustion.Coal dust semicoke after stripping is after partial combustion, by the charcoal of burning-off 40%～60%.
In step D, in riser tube gasifying reactor 2, be 3～10s (second) with atomized water steam 133 with the time that gasification water vapor 202 carries out water-gas reaction through partially combusted coal dust semicoke, the temperature of riser tube gasifying reactor 2 top exits is lower 30～60 DEG C than the temperature of bottom inlet, and the working pressure of riser tube gasifying reactor 2 top exits is 0.1～0.4MPa.The temperature of riser tube gasifying reactor 2 bottom inlets, is substantially equal to the temperature of combustion in gasification combustor 11.
In step e, the medial temperature of the interior coal ash dense-phase bed of coal ash coal gas separator 1 is 650～750 DEG C, and the working pressure at coal ash coal gas separator 1 top is 0.1～0.4MPa, and the linear gas velocity of coal ash coal gas separator 1 dilute phase section is 0.2～1.2m/s.Gas in described linear gas velocity is mainly the fluidizing agent 5 (being fluidized in addition the residual gas that the coal ash in gas 5 strippings coal ash dense-phase bed is out carried secretly) that enters coal ash coal gas separator 1 dilute phase section.
The diameter of coal ash coal gas separator 1 top cylinder shape cylindrical shell is mainly according to the mobility scale calculative determination of coal ash coal gas separator 1 dilute phase section linear gas velocity, the height of coal ash dense-phase bed is mainly according to the reserve calculative determination of coal ash coal gas separator 1 interior coal ash, and the height of coal ash coal gas separator 1 dilute phase section is mainly according to the settling height calculative determination of coal ash.
In operating process, a part of high temperature coal ash in interior coal ash coal gas separator 1 coal ash dense-phase bed is sent into external warmer 22 through cement output tank 221, through external warmer 22 heat-obtainings, be cooled to 70～80 DEG C.Heat-obtaining, cooled coal ash, a part is wherein returned to coal ash dense-phase bed through return tube 222, at 650～750 DEG C, is no more than the temperature range of regulation with the medial temperature of controlling coal ash dense-phase bed.Through external warmer 22 heat-obtainings, cooled another part coal ash, after pipeline 223 enters coal ash tank 21, destructive distillation device is discharged in timing.
Claims (10)
1. a fluidized bed dry distillation method for coal dust, is characterized in that: the method in turn includes the following steps:
A. the coal dust raw material (150) after pulverizing enters the bottom of coal dust raw material preheating pipe (12) through coal dust material feeding tube (15), up along coal dust raw material preheating pipe (12) under the effect of the lift gas (140) being passed into by lift gas jet pipe (14), the heat that coal dust semicoke after absorption stripping carries out combustion reactions generation in gasification combustor (11) carries out preheating, and the coal dust raw material (150) after preheating enters bed formula fluidized bed dry distillation reactor (9) through coal dust raw material riser tube (10);
B. in the close phase section of the destructive distillation bed of coal dust raw material (150) in bed formula fluidized bed dry distillation reactor (9), carry out dry distillation reactor, generate oil gas and coal dust semicoke, the first group cyclonic separator (8) of oil gas in being located at bed formula fluidized bed dry distillation reactor (9) isolated the defocused oil gas vent pipe (7) by bed formula fluidized bed dry distillation reactor (9) top of coal dust half and flowed out, coal dust semicoke in the close phase section of destructive distillation bed flows downward, enter the stripper (18) of being located at bed formula fluidized bed dry distillation reactor (9) below, in stripper (18), pass into water stripping steam (170), stripping goes out coal dust semicoke entrained oil gas,
C. in stripper (18), the coal dust semicoke after stripping enters gasification combustor (11) through coal dust semicoke transfer lime (16), carry out combustion reactions with the oxygen (132) in combustion gases sparger (13) passes into gasification combustor (11), the carbon monoxide, carbonic acid gas generating after burning carrying together with atomized water steam (133) that pass through partially combusted coal dust semicoke upwards mobile, enters riser tube gasifying reactor (2);
D. in riser tube gasifying reactor (2), enter the partially combusted coal dust semicoke of process and the atomized water steam (133) in riser tube gasifying reactor (2) and pass into the interior gasified water steam (202) of riser tube gasifying reactor (2) along the up water-gas reaction of carrying out of riser tube gasifying reactor (2), the coal gas of generation and high temperature coal ash enter coal ash coal gas separator (1);
E. in coal ash coal gas separator (1), coal gas and high temperature coal ash carry out gas solid separation in second group of cyclonic separator (24), and isolated coal gas is flowed out by the gas outlet tube (26) at coal ash coal gas separator (1) top.
2. method for destructive distillation according to claim 1, is characterized in that: in steps A, coal dust raw material (150) temperature after preheating in coal dust raw material preheating pipe (12) is 450～550 DEG C.
3. method for destructive distillation according to claim 2, it is characterized in that: in step B, the dry distillation reactor time of coal dust raw material (150) in the close phase section of destructive distillation bed is 2～10min, the temperature of the close phase section of destructive distillation bed is 450～550 DEG C, the working pressure at bed formula fluidized bed dry distillation reactor (9) top is 0.1～0.4MPa, the linear gas velocity of bed formula fluidized bed dry distillation reactor (9) dilute phase section is 0.2～1.2m/s, the coal dust semicoke that is gone out to carry secretly oil gas in stripper (18) by stripping, its carbon content is 65%～85%.
4. method for destructive distillation according to claim 3, it is characterized in that: in step C, the time that coal dust semicoke burns in gasification combustor (11) is 3～5min, temperature of combustion is 800～900 DEG C, the working pressure at gasification combustor (11) top is 0.15～0.5MPa, coal dust semicoke is after partial combustion, by the charcoal of burning-off 40%～60%.
5. method for destructive distillation according to claim 4, it is characterized in that: in step D, riser tube gasifying reactor (2) in, be 3～10s with the time that atomized water steam (133) and the water vapor (202) that gasifies carry out water-gas reaction through partially combusted coal dust semicoke, the temperature of riser tube gasifying reactor (2) top exit is lower 30～60 DEG C than the temperature of bottom inlet, and the working pressure of riser tube gasifying reactor (2) top exit is 0.1～0.4MPa.
6. according to the method for destructive distillation described in any one in claim 1 to 5, it is characterized in that: a part of high temperature coal ash in the interior coal ash dense-phase bed of coal ash coal gas separator (1) through external warmer (22) heat-obtaining, cooling after, a part is wherein returned to coal ash dense-phase bed.
7. according to the method for destructive distillation described in any one in claim 1 to 5, it is characterized in that: coal dust raw material (150) is brown coal, long-flame coal, bottle coal, non-caking coal or weakly caking coal, and its particle diameter is not more than 3mm.
8. one kind for realizing the fluidized bed dry distillation device of the coal dust of method described in claim 1, be provided with fluidized bed dry distillation reactor, Pyrolysis Char burning and gasifying reactor, fluidized bed dry distillation reactor is provided with coal dust material feeding tube (15), it is characterized in that: dry distillation reactor device is bed formula fluidized bed dry distillation reactor (9), in it, be provided with first group of cyclonic separator (8), top is provided with oil gas collection chamber (6), oil gas vent pipe (7), below is coaxially arranged with stripper (18) with it, stripper is provided with stripping baffles in (18), bottom is provided with stripped vapor sparger (17), Pyrolysis Char burning comprises gasification combustor (11) and riser tube gasifying reactor (2) with gasifying reactor, gasification combustor (11) is positioned at the below of riser tube gasifying reactor (2), the housing of gasification combustor (11) comprises the cylindrical drum of bottom and the round table surface shape cylindrical shell on top, between the bottom bulkhead of the side of cylindrical drum and stripper (18), be provided with coal dust semicoke transfer lime (16), in gasification combustor (11), be coaxially arranged with coal dust raw material preheating pipe (12) with it, the bottom of coal dust raw material preheating pipe (12) is stretched out by the bottom of gasification combustor (11), described coal dust material feeding tube (15) is located at the bottom of coal dust raw material preheating pipe (12), the bottom of coal dust raw material preheating pipe (12) is provided with lift gas jet pipe (14), the top exit of coal dust raw material preheating pipe (12) is connected with pipe connecting (20), pipe connecting (20) is stretched out by gasification combustor (11), its top exit is connected with the bottom inlet of coal dust raw material riser tube (10), the top exit of coal dust raw material riser tube (10) is connected with horizontal pipeline section (101), the outlet (102) of horizontal pipeline section (101) is positioned at the dilute phase section of bed formula fluidized bed dry distillation reactor (9), the bottom of gasification combustor (11) is provided with combustion gases sparger (13), combustion gases sparger (13) is connected with inlet pipe (131), inlet pipe (131) is with oxygen intake and atomized water steam-in, riser tube gasifying reactor (2) is the rounded vertical tube of cross section, its bottom inlet is connected with the top exit of gasification combustor (11), bottom is provided with gasified water steam inlet tube (201), the top of bed formula fluidized bed dry distillation reactor (9) is provided with coal ash coal gas separator (1), in it, be provided with second group of cyclonic separator (24), the top exit of riser tube gasifying reactor (2) is connected with second group of cyclonic separator (24) by one section of level pipe (203), the top of coal ash coal gas separator (1) is provided with coal gas collection chamber (25), gas outlet tube (26), bottom is provided with fluidizing agent sparger (4).
9. destructive distillation device according to claim 8, it is characterized in that: coal ash coal gas separator (1) is provided with external warmer (22), between external warmer (22) and coal ash coal gas separator (1), be provided with cement output tank (221) and return tube (222).
10. destructive distillation device according to claim 8 or claim 9, it is characterized in that: the height a of gasification combustor (11) is 2～10m, the diameter of cylindrical drum is 1000～5000mm, the height h of riser tube gasifying reactor (2) is 10～40m, and riser tube gasifying reactor (2) is 20%～50% of gasification combustor 11 cylindrical drum cross-sectional areas with the cross-sectional area of coal dust raw material preheating pipe 12.
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