CN103242907B - High-pressure multistage fluidized bed reactor - Google Patents
High-pressure multistage fluidized bed reactor Download PDFInfo
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Abstract
The invention discloses a high-pressure multistage fluidized bed reactor which comprises multiple container bodies, wherein the container body is provided with a gasification chamber, and each gasification chamber is provided with an air inlet, a feed inlet, an air outlet and a discharge outlet; the most downstream last-stage gasification chamber is also provided with a fluidized gas inlet connected with a fluidized gas source; and in adjacent two gasification chambers, the air inlet of the upstream gasification chamber and the air outlet of the downstream gasification chamber are connected through a gas conveying pipe outside the container body, the discharge outlet of the upstream gasification chamber and the feed inlet of the downstream gasification chamber are connected through a feeding pipe outside the container body; and the feed inlet of the most upstream first-stage gasification chamber is connected with a raw material coal source through a high-pressure coal-oil slurry pump or a high-pressure pulverized coal pump, and the air inlet of the last-stage gasification chamber is connected with a gasification agent source. The high-pressure multistage fluidized bed reactor disclosed by the invention is simple in structure, convenient to manufacture, large in capacity, high in operating pressure, good in fluidized bed fluidization effect, and high in gasification efficiency.
Description
Technical field
The present invention relates to Coal Gasification Technology, especially relate to a kind of high-pressure multi-stage fluidized-bed reactor.
Background technology
By the PC-FB producing synthesis gas developing history of existing more than 80 year, what the vapourizing furnace of this type of great majority obtained is all low-heat value gas or the synthetic gas of co hydrogenation gas, is mainly used in the Chemical Manufacture of synthetic ammonia or methyl alcohol.A normally straight barrel type vapourizing furnace of tradition fluidized-bed gasification furnace, coal dust adds from the bottom of vapourizing furnace, the high-temperature flue gas that vapourizing furnace produces adopts the mode of indirect heat exchange to reclaim heat, cause system heat-exchange equipment many, facility investment is large, system flow is long, equipment failure point is many, causes system cannot realize long-period stable operation.Operating pressure is low, and production capacity is low.There is in the recent period people to obtain by the method for PC-FB catalytic gasification the synthetic gas that is rich in methane.
Chinese invention patent application CN102399595 discloses a kind of multilayer fluidized bed gasification furnace.But there is following problem in this multilayer fluidized bed gasification furnace:: in body of heater, be provided with three layers or above multistage vaporizer, the body of heater excessive height while causing single stove to maximize and strengthened the difficulty of device fabrication, installation and dimension inspection; The overflow device of tubulose is located in furnace chamber, and the formation of every laminarization bed is existed to disadvantageous effect, all bears high temperature inside and outside upflow tube, high to material requirements, and is not easy to change and maintenance.
Summary of the invention
The object of the invention is to propose a kind of non-catalytic mode, utilize fluidized-bed gasification mode that high pressure, multistage different gasification temperatures combine to obtain the synthetic gas of the high methane of high hydrogen, the high-pressure multi-stage fluidized-bed reactor that have simple in structure, easy maintenance, hold maximization, fluidized-bed fluid effect at different levels is good and gasification efficiency is high, working pressure reaches as high as 9.0MPa.
For achieving the above object, high-pressure multi-stage fluidized-bed reactor according to the present invention comprises: multiple container bodys that order arranges, have the vaporizer that is used to form fluidized-bed in each described container body; Each described vaporizer all has inlet mouth, opening for feed, air outlet and discharge port; The final stage vaporizer that is positioned at downstream is also provided with the inlet for fluidization air being connected with fluidisation source of the gas; In adjacent two vaporizers, the inlet mouth that is positioned at the vaporizer of upstream is connected by the pneumatic tube that is positioned at described container body outside with the air outlet of the vaporizer that is positioned at downstream, the discharge port that is positioned at the vaporizer of upstream is connected by the carrier pipe that is positioned at described container body outside with the opening for feed of the vaporizer that is positioned at downstream, the inlet mouth of wherein said final stage vaporizer is connected with vaporized chemical source, and the opening for feed that is positioned at the chopped-off head vaporizer of upstream is connected with feed coal source by high-pressure oil coal slurry pump or high pressure coal dust pump.
According to high-pressure multi-stage fluidized-bed reactor of the present invention, the upstream indoor material that gasifies is transported to adjacent downstream vaporizer by the pipeline that is positioned at container body outside, not only, in container body, there is no Material pipeline, can not cause disadvantageous effect to the formation of fluidized-bed, and, above-mentioned material pipe is positioned at container body outside, high temperature is not born in pipeline outside, low to material rate requirement, and is easy to change and maintenance.According to high-pressure multi-stage fluidized-bed reactor of the present invention, material and gas is counter current contact in vaporizers at different levels, and therefore gasification result is good, can not add material to affect gasification result because of the downstream vaporizer from being positioned at chopped-off head vaporizer.
Preferably, high-pressure multi-stage fluidized-bed reactor also comprises gas-solid separator, and described gas-solid separator has air outlet, semicoke returning charge outlet and the inlet mouth being connected with the air outlet of described chopped-off head vaporizer; On the sidewall of described final stage vaporizer, be also provided with described semicoke returning charge and export the semicoke opening for feed being connected, the semicoke opening for feed of described final stage vaporizer is connected by fluidized gas, the semicoke returning charge that comes from described semicoke returning charge outlet to be transported in described final stage vaporizer with described fluidisation source of the gas.
Preferably, in the opening for feed of described chopped-off head vaporizer, be provided with the feed coal nozzle stretching in described chopped-off head vaporizer, in the inlet mouth of described vaporizer, be provided with the gas distributor extending in this vaporizer, in described inlet for fluidization air, be provided with the fluidized gas sparger extending in described final stage vaporizer.
Preferably, described feed coal nozzle is multiple and is uniformly distributed along the circumferential interval of described chopped-off head vaporizer.
Preferably, the lower isolation of described final stage vaporizer goes out fluidisation air chamber, the inlet mouth of described final stage vaporizer is connected with described vaporized chemical source, the inlet for fluidization air of described final stage vaporizer is arranged on the sidewall of described fluidisation air chamber, and the air outlet of the each vaporizer between described chopped-off head vaporizer and described final stage vaporizer is arranged on the top or sidewall of this vaporizer.
Preferably, except described chopped-off head vaporizer, the opening for feed of all the other all vaporizers is all connected with described fluidisation source of the gas with the semicoke mass transport the vaporizer discharge port from upstream sent by fluidized gas in the vaporizer in adjacent downstream.
Preferably, the discharge port of described final stage vaporizer is arranged in the bottom of the sidewall of described final stage vaporizer.
Preferably, the internal surface of described carrier pipe and described pneumatic tube is provided with wear-resisting and adiabatic lining.
Preferably, on described carrier pipe and described pneumatic tube, be equipped with variable valve and introduce the access port of fluidized gas;
Preferably, the internal surface of described container body is provided with wear-resisting and adiabatic lining.
Preferably, multiple described container bodys arrange along the vertical direction or along continuous straight runs arrange or along the vertical direction with horizontal direction mix arrange.
Preferably, the fluidized gas that described fluidisation source of the gas is supplied with is at least one in steam, oxygen, synthetic gas, carbonic acid gas.
Preferably, described feed coal is sent into described chopped-off head vaporizer after mixing with benzene class I liquid I material, and described benzene class I liquid I material is the by product of described high-pressure multi-stage fluidized-bed reactor.
Preferably, the gasification operation pressure in described container body is 1.0-9.0MPa.
Brief description of the drawings
Fig. 1 is the schematic diagram of high-pressure multi-stage fluidized-bed reactor according to an embodiment of the invention.
Fig. 2 is the schematic diagram of high-pressure multi-stage fluidized-bed reactor according to another embodiment of the present invention.
Embodiment
Below with reference to accompanying drawing, embodiments of the invention are described.
As depicted in figs. 1 and 2, high-pressure multi-stage fluidized-bed reactor according to the present invention comprises multiple container bodys 100 that order arranges, and in each container body 100, is formed with vaporizer, and vaporizer is for forming fluidized-bed therein.Preferably, container body 100 is preferably obround vessel, and the internal surface of container body 100 is provided with wear-resisting and adiabatic lining (not shown).
Be understandable that, in description of the invention, edge and the gas direction that flow direction is contrary between multiple container bodys 100, what be positioned at container body above is upstream container body, the container body being positioned at is below downstream reservoir body, for example be positioned at the top container body 100 being connected with feed coal source and can be called chopped-off head container body, vaporizer in chopped-off head container body can be called chopped-off head vaporizer, fluidized-bed in chopped-off head vaporizer can be called chopped-off head fluidized-bed, be positioned at the rearmost container body 100 being connected with fluidisation source of the gas and can be called final stage container body, vaporizer in final stage container body can be called final stage vaporizer, fluidized-bed in final stage vaporizer can be called final stage fluidized-bed, therefore, along the direction from chopped-off head container body to final stage container body, one side of contiguous chopped-off head container body is upstream, one side of contiguous final stage container body is downstream.
In specific embodiments of the invention, multiple container bodys 100 can be arranged along the vertical direction or horizontal direction is arranged.
Each vaporizer has inlet mouth, opening for feed, air outlet and discharge port.Final stage vaporizer also has the inlet for fluidization air being connected with fluidisation source of the gas 400, and the fluidized gas that fluidisation source of the gas 400 is supplied with can be at least one in steam, oxygen (pure oxygen, oxygen-rich air, air), synthetic gas and carbonic acid gas.In adjacent two vaporizers, the inlet mouth that is positioned at the vaporizer of upstream is connected by the pneumatic tube that is positioned at container body 100 outsides with the air outlet of the vaporizer that is positioned at downstream, and the discharge port that is positioned at the vaporizer of upstream is connected by the carrier pipe that is positioned at described container body outside with the opening for feed of the vaporizer that is positioned at downstream.Preferably, the internal surface of described carrier pipe and described pneumatic tube is provided with wear-resisting and adiabatic lining (not shown).More preferably, on described carrier pipe and described pneumatic tube, be equipped with variable valve 500 and introduce the access port of fluidized gas, be convenient to the adjusting of material and gas.
The inlet mouth of final stage vaporizer is connected with vaporized chemical source 300, and the opening for feed of chopped-off head vaporizer is connected with feed coal source by high-pressure oil coal slurry pump or high pressure coal dust pump.The discharge port of final stage vaporizer, for deslagging, therefore also can be called slag notch, and the discharge port of final stage vaporizer can be arranged in the bottom of the sidewall of final stage vaporizer.Preferably, the feed coal that described feed coal source is supplied with can be sent into described chopped-off head vaporizer with after benzene class I liquid I material mixes, and described benzene class I liquid I material can be according to the by product of the described high-pressure multi-stage fluidized-bed reactor of the embodiment of the present invention.
In some embodiments of the invention, the gasification operation pressure in high-pressure multi-stage fluidized-bed reactor can be in the scope of 1.0-9.0MPa, and compared with traditional fluidized-bed reactor, pressure can improve greatly.In an embodiment of the present invention, " high pressure " can be for being greater than the pressure of 1.0MPa.
According to the high-pressure multi-stage fluidized-bed reactor of the embodiment of the present invention, comprise multiple container bodys 100, be positioned at container body 100 outsides for the carrier pipe of material conveying between container body 100 and the pneumatic tube of delivering gas, can not cause disadvantageous effect to the fluidized-bed in the vaporizer in container body 100, and, because carrier pipe and pneumatic tube are positioned at container body 100 outsides, can not bear the high temperature in vaporizer, reduce the requirement of the material to carrier pipe and pneumatic tube, reduce cost, and replacing and easy to maintenance.In addition, because multiple container bodys 100 can sequentially be arranged independently of one another, therefore, can need along the vertical direction according to technique,, horizontal direction or upper and lower and horizontal direction mix and arrange container body 100.Here, mix and arrange along upper and lower and horizontal direction, refer to the vertical central axis alignment of a part of container body 100, the vertical central axis of another part container body 100 is parallel to each other and along continuous straight runs is spaced apart, in addition, the vertical central axis of described a part of container body 100 and the central axis of another part container body 100 on above-below direction mistake can, example as shown in Figure 1.
Preferably, also comprise gas-solid separator 200 according to the high-pressure multi-stage fluidized-bed reactor of the embodiment of the present invention, gas-solid separator 200 has air outlet 202, semicoke returning charge outlet 203 and the inlet mouth 201 being connected with the air outlet of chopped-off head vaporizer.On the sidewall of final stage vaporizer, be also provided with semicoke returning charge and export the 203 semicoke opening for feeds that are connected, the semicoke opening for feed of final stage vaporizer is connected by fluidized gas, the semicoke returning charge that comes from semicoke returning charge outlet 203 to be transported in final stage vaporizer with fluidisation source of the gas 400.
Preferably, in the opening for feed of chopped-off head vaporizer, be provided with the feed coal nozzle stretching in chopped-off head vaporizer, in the inlet mouth of each vaporizer, be provided with the gas distributor extending in this vaporizer, in inlet for fluidization air 119, be provided with the fluidized gas sparger extending in described final stage vaporizer.Feed coal nozzle is multiple and is uniformly distributed along the circumferential interval of described chopped-off head vaporizer.
In some embodiments of the invention, the lower isolation of final stage vaporizer goes out fluidisation air chamber E, the inlet mouth of described final stage vaporizer is connected with vaporized chemical source 300, the inlet for fluidization air of final stage vaporizer is arranged on the sidewall of fluidisation air chamber E, and the air outlet of the each vaporizer between chopped-off head vaporizer and final stage vaporizer is arranged on the top or sidewall of this vaporizer.
Preferably, except described chopped-off head vaporizer, the opening for feed of all the other all vaporizers is all connected with fluidisation source of the gas 400 with the semicoke mass transport the vaporizer discharge port from upstream sent by fluidized gas in the vaporizer in adjacent downstream.
In a preferred embodiment of the invention, on carrier pipe and pneumatic tube, be equipped with variable valve and introduce the access port that fluidized gas enters.
Below with reference to Fig. 1, high-pressure multi-stage fluidized-bed reactor is according to an embodiment of the invention described.In the embodiment shown in fig. 1, high-pressure multi-stage fluidized-bed reactor comprises four container bodys 100, that is: chopped-off head container body, second stage container body, third stage container body and final stage container body.In chopped-off head container body, be formed with in chopped-off head vaporizer A(chopped-off head vaporizer A and be formed with chopped-off head fluidized-bed, in description of the invention, term " vaporizer " can exchange use with " fluidized-bed "), in the container body of the second stage, be formed with in the vaporizer of the vaporizer B(second stage, the second stage and be formed with second stage fluidized-bed), in third stage container body, be formed with in third stage vaporizer C(third stage vaporizer and be formed with third stage fluidized-bed), in final stage level container body, be formed with in final stage vaporizer D(final stage vaporizer and be formed with final stage fluidized-bed).
In the embodiment shown in fig. 1, chopped-off head container body and second stage container body are arranged along the vertical direction, it is the vertical central axes of vertical central axis and the second stage container body of chopped-off head container body, third stage container body and final stage container body are arranged along the vertical direction, be the vertical central axes of vertical central axis and the final stage container body of third stage container body, and the vertical central axis of chopped-off head container body and the vertical central axis of final stage container body spaced apart in the horizontal direction.
In other words, four interior formation orders of container body 100 are arranged four vaporizer A-D, form respectively chopped-off head fluidized-bed, second stage fluidized-bed, third stage fluidized-bed and final stage fluidized-bed in four vaporizers.
The upper portion side wall of chopped-off head vaporizer (also can be called chopped-off head fluidized-bed) A is provided with chopped-off head fluidized-bed opening for feed 102, in chopped-off head fluidized-bed opening for feed 102, be provided with feed coal nozzle 130, can in chopped-off head vaporizer A, supply with coal dust or benzene class coal oil mixture material by chopped-off head fluidized-bed opening for feed 102.Coal dust or benzene class coal oil mixture material are injected in chopped-off head vaporizer A by feed coal nozzle 130, can improve thus gasification result.More preferably, feed coal nozzle 130 is multiple and is uniformly distributed along the circumferential interval of chopped-off head vaporizer A, can further improve thus gasification result.
The roof of chopped-off head vaporizer A is provided with the syngas outlet 101 on the vertical central axis that is positioned at container body 100, the gas producing in chopped-off head vaporizer A can be discharged chopped-off head vaporizer A by syngas outlet 101, because syngas outlet 101 is positioned on the vertical central axis of container body 100, therefore, the discharge of synthetic gas is more smooth and easy, and the fluidized-bed in vaporizers at different levels is not existed to disadvantageous effect.The lower sides of chopped-off head vaporizer A is provided with chopped-off head discharging port of fluidized bed 104, and the material in chopped-off head vaporizer A is discharged from chopped-off head discharging port of fluidized bed 104.The sidewall of chopped-off head vaporizer A is provided with chopped-off head fluidized-bed inlet mouth 103.
The roof of second stage vaporizer B is provided with fluidized-bed air outlet, the second stage 105, the sidewall of second stage vaporizer B is provided with second stage fluidized-bed opening for feed 106, the sidewall of second stage vaporizer B is provided with the second stage fluidized-bed inlet mouth 107 that the pneumatic tube by being positioned at container body 100 outsides is communicated with the third stage fluidized-bed air outlet 109 of third stage vaporizer C, the access port that pneumatic tube is provided with variable valve 500 and enters for introducing fluidized gas, gas in third stage vaporizer C enters second stage vaporizer B by second stage fluidized-bed inlet mouth 107, so that the fluidized-bed in the vaporizer B of the second stage forms and the generation of synthetic gas, the sidewall of second stage vaporizer B is provided with second stage discharging port of fluidized bed 108, material in the vaporizer B of the second stage is discharged from second stage discharging port of fluidized bed 108.
The roof of third stage vaporizer C is provided with third stage fluidized-bed air outlet 109, the sidewall of third stage vaporizer C is provided with by being positioned at container body 100 outsides and being provided with the pneumatic tube of variable valve 500 and third stage fluidized-bed inlet mouth 113 that the final stage fluidized-bed air outlet 114 of final stage vaporizer D is communicated with, gas in final stage fluidized-bed D enters third stage vaporizer C by final stage fluidized-bed air outlet 114 and third stage fluidized-bed inlet mouth 113, so that the fluidized-bed in third stage vaporizer C forms and the generation of synthetic gas.The sidewall of third stage vaporizer C is provided with third stage discharging port of fluidized bed 111 and third stage fluidized-bed opening for feed 112.
The roof of final stage vaporizer D is provided with final stage fluidized-bed air outlet 114, the sidewall of final stage fluidized-bed D is provided with final stage fluidized bed semicoke returning charge opening for feed 115, the sidewall of final stage vaporizer D is provided with final stage fluidized-bed opening for feed 116, the lower sides of final stage fluidized-bed is provided with final stage fluidized-bed inlet mouth (being connected with liquid agent source 300) 118, final stage discharging port of fluidized bed (being grey slag notch) 117 and inlet for fluidization air 119 for being connected with fluidisation source of the gas 400, final stage fluidized-bed opening for feed 116 is communicated with by the carrier pipe that is positioned at container body 100 outsides with third stage discharging port of fluidized bed 111, carrier pipe is provided with variable valve 500 and introduces the access port that fluidized gas enters.Preferably, grey slag notch 117 is arranged in the lower sidewall of final stage container body 100, the discharge of the lime-ash of being more convenient for thus.
Final stage fluidized-bed inlet mouth 118 is connected with vaporized chemical source 300, for supply with vaporized chemical in final stage vaporizer D.Inlet for fluidization air 119 is connected with fluidisation source of the gas 400, for supply with fluidized gas in final stage vaporizer D.
In vaporized chemical import 118, be provided with vaporized chemical sparger, in inlet for fluidization air 119, be provided with fluidized gas sparger 119, so that the fluidized-bed in vaporizer at different levels forms and improve gasification result.
The bottom of final stage vaporizer D for example isolates fluidisation air chamber E by dividing plate, and inlet for fluidization air 119 is formed on the sidewall of final stage fluidisation air chamber D, and the top of final stage fluidisation air chamber D is provided with the pore 120 being communicated with final stage vaporizer D.
Preferably, second stage fluidized-bed opening for feed 106 is connected with fluidisation source of the gas 400, thus can by fluidized gas by the semicoke mass transport of discharging from chopped-off head discharging port of fluidized bed 104 in the vaporizer B of the second stage.Third stage fluidized-bed opening for feed 112 is connected with fluidisation source of the gas 400, thus can by fluidized gas by the semicoke mass transport going out from second stage discharging port of fluidized bed 108 in third stage vaporizer C; Final stage fluidized-bed opening for feed 116 be connected with fluidisation source of the gas 400 with by fluidized gas by the semicoke mass transport going out from third stage discharging port of fluidized bed 111 in final stage vaporizer D.
In a preferred embodiment of the invention, high-pressure multi-stage fluidized-bed reactor also comprises gas-solid separator 200, and gas-solid separator 200 has the inlet mouth 201, air outlet 202 and the semicoke returning charge outlet 203 that are communicated with the syngas outlet 101 of chopped-off head vaporizer A.
On the sidewall of final stage vaporizer D, be also provided with semicoke returning charge and export the 203 semicoke returning charge imports 115 that are connected, semicoke returning charge import 115 be connected with fluidisation source of the gas 400 with by fluidized gas by the semicoke mass transport that comes from semicoke returning charge outlet 203 in final stage vaporizer D.
Thus, enter gas-solid separator 200 from the synthetic gas of chopped-off head container body 100 interior discharges and carry out gas solid separation, the returning charge of isolated solid semicoke is discharged from semicoke returning charge outlet 203, be transported in final stage fluidized-bed D by fluidized gas by semicoke returning charge import 115, improve utilization of materials, reduced and pollute.
According to the high-pressure multi-stage fluidized-bed reactor of the embodiment of the present invention, vaporized chemical and fluidized gas are along from downstream, upstream direction flows, material is along from upstream, direction downstream flows, and material is carried by the carrier pipe that is positioned at container body 100 outsides, gas is carried by the pneumatic tube that is positioned at container body 100 outsides, in container body 100, there is no carrier pipe and pneumatic tube, can not affect the fluidisation of the fluidized-bed in vaporizers at different levels, reduce the requirement to carrier pipe and pneumatic tube material, reduce cost, be convenient to safeguard and change.
According to the high-pressure multi-stage fluidized-bed reactor of the embodiment of the present invention, have that H2, CH4 content in synthetic gas is high, gasification efficiency and a high feature of efficiency of carbon conversion.
According to the high-pressure multi-stage fluidized-bed reactor of the embodiment of the present invention, coal dust or benzene class coal oil mixture material are pressurizeed by spray into chopped-off head vaporizer A at the nozzle on container body top by pump, in the process declining at material, synthetic air-flow rises to the first fluidized bed dryer section in chopped-off head vaporizer A, and material is carried out to preheating, dry, destructive distillation.Semicoke after preheating is by entering the second fluidized-bed in the vaporizer B of the second stage the synthesis gas reaction with hydrogen rich gas, and semicoke is converted to the synthetic gas that is rich in methane.Semicoke in the vaporizer B of the second stage after gasification enters in the 3rd fluidized-bed in third stage vaporizer C, and react with the synthesis gas of the final stage fluidized-bed from final stage vaporizer D, at the 3rd vaporizer, steam reacts the synthetic gas that generates H2, CO etc. and be rich in methane with the carbon in material semicoke.Semicoke after the 3rd vaporizer gasification enters in final stage vaporizer, and for example, to react generation major ingredient with carbon with the steam-oxygen (, pure oxygen, oxygen-rich air, air) from downstream vaporizer be the synthetic gas of H2 and CO.Thus, coal dust or benzene class slurry are entering after high-pressure multi-stage fluidized-bed reactor elder generation and steam-oxygen reaction, repeatedly fully contact and react with synthetic gas again, improve heat transfer rate, extend the residence time of pulverized coal particle in vapourizing furnace, improved the H2 in synthetic gas, CH4 content is high, thereby significantly improve efficiency of carbon conversion.
According to the high-pressure multi-stage fluidized-bed reactor of the embodiment of the present invention, the transformation efficiency of carbon can reach more than 95%, the rate of decomposition of water vapour can be up to more than 60%, CH4 content in synthetic gas can reach more than 15%, H2 content can reach more than 35%, there is significant gasification efficiency, can be widely used in existing producing synthesis gas from coal or fuel gas gasification technology field.
Fig. 2 shows high-pressure multi-stage fluidized-bed reactor according to another embodiment of the present invention, as shown in Figure 2, compared with the embodiment shown in Fig. 1, difference is that four container bodys 100 arrange along the vertical direction, and the vertical central axis of four container bodys 100 overlaps each other.Shown in high-pressure multi-stage fluidized-bed reactor embodiment illustrated in fig. 2 and Fig. 1, other structures of high-pressure multi-stage fluidized-bed reactor and class of operation seemingly, are not described in detail here.
Have the following advantages according to the high-pressure multi-stage fluidized-bed reactor of the embodiment of the present invention, 1) by adopting nozzle ejection material, strengthened the mixed effect of semicoke and hydrogen-rich synthetic gas in vaporizer, mass transfer, rate of heat transfer are high, effectively reduce the content of grey combustibles in the slag; 2) material of gasification flows in multiple vaporizers, H2, CO, CH4 in high, the effective gas of gas forming amount of unit mass coal dust, wherein efficiency of carbon conversion is up to more than 95%, CH4 content in synthetic gas can reach more than 15%, H2 content can reach more than 35%, and the rate of decomposition of water vapour is up to more than 60%; 3) import and export of fluidized-beds at different levels for example, are communicated with by the carrier pipe and the pneumatic tube (riser tube, tremie pipe, scum pipe, air inlet and escape pipe) that are positioned at container body outside, and the internal surface of pipe is provided with wear-resisting and adiabatic lining, extend the work-ing life of material pipeline, convenient maintenance, has improved the online rate of installing; 4) reactor is simple in structure, and reliability is high, stable, and production capacity is large, therefore has the wider scope of application.
Although illustrated and described embodiments of the invention above, be understandable that, above-described embodiment can not be interpreted as limitation of the present invention, but can have many modification.
Claims (12)
1. a high-pressure multi-stage fluidized-bed reactor, is characterized in that, comprises four container bodys that order arranges, and in each described container body, has the vaporizer that is used to form fluidized-bed; Each described vaporizer all has inlet mouth, opening for feed, air outlet and discharge port; The final stage vaporizer that is positioned at downstream is also provided with the inlet for fluidization air being connected with fluidisation source of the gas; In adjacent two vaporizers, the inlet mouth that is positioned at the vaporizer of upstream is connected by the pneumatic tube that is positioned at described container body outside with the air outlet of the vaporizer that is positioned at downstream, the discharge port that is positioned at the vaporizer of upstream is connected by the carrier pipe that is positioned at described container body outside with the opening for feed of the vaporizer that is positioned at downstream, the opening for feed that is wherein positioned at the chopped-off head vaporizer of upstream is connected with feed coal source by high-pressure oil coal slurry pump or high pressure coal dust pump, and the inlet mouth of described final stage vaporizer is connected with vaporized chemical source;
The lower isolation of described final stage vaporizer goes out fluidisation air chamber, the inlet mouth of described final stage vaporizer is connected with described vaporized chemical source, the inlet for fluidization air of described final stage vaporizer is arranged on the sidewall of described fluidisation air chamber, and the air outlet of the each vaporizer between described chopped-off head vaporizer and described final stage vaporizer is arranged on the top or sidewall of this vaporizer;
Except described chopped-off head vaporizer, the opening for feed of all the other all vaporizers is all connected with described fluidisation source of the gas with the semicoke mass transport the vaporizer discharge port from upstream sent by fluidized gas in the vaporizer in adjacent downstream.
2. high-pressure multi-stage fluidized-bed reactor according to claim 1, is characterized in that, also comprises gas-solid separator, and described gas-solid separator has air outlet, semicoke returning charge outlet and the inlet mouth being connected with the air outlet of described chopped-off head vaporizer; On the sidewall of described final stage vaporizer, be also provided with described semicoke returning charge and export the semicoke opening for feed being connected, the semicoke opening for feed of described final stage vaporizer is connected by fluidized gas, the semicoke returning charge that comes from described semicoke returning charge outlet to be transported in described final stage vaporizer with described fluidisation source of the gas.
3. high-pressure multi-stage fluidized-bed reactor according to claim 1, it is characterized in that, in the opening for feed of described chopped-off head vaporizer, be provided with the feed coal nozzle stretching in described chopped-off head vaporizer, in the inlet mouth of described vaporizer, be provided with the gas distributor extending in this vaporizer, in described inlet for fluidization air, be provided with the fluidized gas sparger extending in described final stage vaporizer.
4. high-pressure multi-stage fluidized-bed reactor according to claim 3, is characterized in that, described feed coal nozzle is multiple and is uniformly distributed along the circumferential interval of described chopped-off head vaporizer.
5. high-pressure multi-stage fluidized-bed reactor according to claim 1, is characterized in that, the discharge port of described final stage vaporizer is arranged in the bottom of the sidewall of described final stage vaporizer.
6. high-pressure multi-stage fluidized-bed reactor according to claim 1, is characterized in that, the internal surface of described carrier pipe and described pneumatic tube is provided with wear-resisting and adiabatic lining.
7. high-pressure multi-stage fluidized-bed reactor according to claim 6, is characterized in that, on described carrier pipe and described pneumatic tube, is equipped with variable valve, is also provided with and introduces the access port that fluidized gas enters on described carrier pipe.
8. high-pressure multi-stage fluidized-bed reactor according to claim 1, is characterized in that, the internal surface of described container body is provided with wear-resisting and adiabatic lining.
9. according to the high-pressure multi-stage fluidized-bed reactor described in any one in claim 1-8, it is characterized in that the arrangement that multiple described container bodys are arranged along the vertical direction or along continuous straight runs is arranged or edge is upper and lower and horizontal direction is mixed.
10. high-pressure multi-stage fluidized-bed reactor according to claim 1, is characterized in that, the fluidized gas that described fluidisation source of the gas is supplied with is at least one in steam, oxygen, synthetic gas and carbonic acid gas.
11. high-pressure multi-stage fluidized-bed reactors according to claim 1, is characterized in that, described feed coal is sent into described chopped-off head vaporizer after mixing with benzene class I liquid I material, and described benzene class I liquid I material is the by product of described high-pressure multi-stage fluidized-bed reactor.
12. high-pressure multi-stage fluidized-bed reactors according to claim 1, is characterized in that, the gasification operation pressure in described container body is 1.0-9.0MPa.
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| CN201310187848.5A CN103242907B (en) | 2013-05-20 | 2013-05-20 | High-pressure multistage fluidized bed reactor |
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| CN103509602A (en) * | 2013-09-24 | 2014-01-15 | 上海鑫兴化工科技有限公司 | Raw material coal conveying method and system for gasification furnace |
| CN104479774B (en) * | 2014-11-10 | 2017-10-27 | 新奥科技发展有限公司 | A kind of device and method of coal gasification methane |
| CN104862015B (en) * | 2015-06-01 | 2017-03-29 | 上海河图工程股份有限公司 | A kind of two sections of temperature control Fossil fuel gasification installations |
| CN105112105A (en) * | 2015-09-02 | 2015-12-02 | 上海尧兴投资管理有限公司 | Gasification coupled system and application thereof |
| CN110016553B (en) * | 2019-02-21 | 2020-09-08 | 张伟晓 | Hot-pressing oxidation leaching system and process |
| CN111575062B (en) * | 2020-04-10 | 2021-06-29 | 华电电力科学研究院有限公司 | Coal heterogeneous catalytic pyrolysis gasification combustion reactor |
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| US4077778A (en) * | 1975-09-29 | 1978-03-07 | Exxon Research & Engineering Co. | Process for the catalytic gasification of coal |
| CN102399595A (en) * | 2010-09-13 | 2012-04-04 | 新奥科技发展有限公司 | Multilayer fluidized bed gasification furnace |
| CN203238228U (en) * | 2013-05-20 | 2013-10-16 | 上海鑫兴化工科技有限公司 | High-pressure multi-level fluidized bed reactor |
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| US4077778A (en) * | 1975-09-29 | 1978-03-07 | Exxon Research & Engineering Co. | Process for the catalytic gasification of coal |
| CN102399595A (en) * | 2010-09-13 | 2012-04-04 | 新奥科技发展有限公司 | Multilayer fluidized bed gasification furnace |
| CN203238228U (en) * | 2013-05-20 | 2013-10-16 | 上海鑫兴化工科技有限公司 | High-pressure multi-level fluidized bed reactor |
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