CN103242907A - High-pressure multistage fluidized bed reactor - Google Patents

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

The high-pressure multi-stage fluidized-bed reactor

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

Produce the existing 80 years of development history of synthetic gas with PC-FB, what the vapourizing furnace of this type of great majority obtained all is 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.The tradition fluidized-bed gasification furnace is a straight barrel type vapourizing furnace normally, 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's heat-exchange equipment many, facility investment is big, system flow is long, equipment failure point is many, causes system can't realize long-period stable operation.System operation pressure is low, and production capacity is low.There is the method for human PC-FB catalytic gasification to obtain to be rich in the synthetic gas of methane in the recent period.

Chinese invention patent application CN102399595 discloses a kind of multicompartment fluidized bed vapourizing furnace.But there is following problem in this multicompartment fluidized bed vapourizing furnace:: be provided with three layers or above multistage vaporizer in the body of heater, the body of heater excessive height when causing single stove to maximize and strengthened the difficulty of device fabrication, installation and dimension inspection; The overflow device of tubulose is located in the furnace chamber, and there is disadvantageous effect in the formation of every laminarization bed, all bears high temperature inside and outside the upflow tube, to the material requirements height, and is not easy to change and maintenance.

Summary of the invention

The objective 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: a plurality of 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 also is provided with the inlet for fluidization air that links to each other with the fluidisation source of the gas; In adjacent two vaporizers, the inlet mouth that is positioned at the vaporizer of upstream links to each other by the pneumatic tube that is positioned at described container body outside with the air outlet of the vaporizer that is positioned at the downstream, the discharge port that is positioned at the vaporizer of upstream links to each other by the carrier pipe that is positioned at described container body outside with the opening for feed of the vaporizer that is positioned at the downstream, the inlet mouth of wherein said final stage vaporizer links to each other with the vaporized chemical source, and the opening for feed that is positioned at the chopped-off head vaporizer of upstream links to each other with the 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, gasification indoor material in upstream arrives adjacent downstream vaporizer by the pipe-line transportation that is positioned at the container body outside, not only, in container body, do not have Material pipeline, can not cause disadvantageous effect to the formation of fluidized-bed, and, above-mentioned material pipe is positioned at the container body outside, high temperature is not born in the pipeline outside, and is low to the material rate requirement, and be 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, so gasification result is good, can not influence gasification result because of adding material from the downstream vaporizer that is positioned at the chopped-off head vaporizer.

Preferably, the high-pressure multi-stage fluidized-bed reactor also comprises gas-solid separator, and described gas-solid separator has the inlet mouth that air outlet, semicoke returning charge outlet links to each other with air outlet with described chopped-off head vaporizer; Also be provided with the semicoke opening for feed that links to each other with described semicoke returning charge outlet on the sidewall of described final stage vaporizer, the semicoke opening for feed of described final stage vaporizer links to each other with described fluidisation source of the gas and is transported in the described final stage vaporizer with the semicoke returning charge that will come from described semicoke returning charge outlet by fluidized gas.

Preferably, be provided with the feed coal nozzle that stretches in the described chopped-off head vaporizer in the opening for feed of described chopped-off head vaporizer, be provided with the gas distributor that extend in this vaporizer in the inlet mouth of described vaporizer, be provided with the fluidized gas sparger that extend in the described final stage vaporizer in the described inlet for fluidization air.

Preferably, described feed coal nozzle is a plurality of and evenly distributes along the circumferential interval of described chopped-off head vaporizer.

Preferably, the lower isolation of described final stage vaporizer goes out the fluidisation air chamber, the inlet mouth of described final stage vaporizer links to each other 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 each vaporizer between described chopped-off head vaporizer and the 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 all links to each other with described fluidisation source of the gas with the semicoke mass transport that will send from the vaporizer discharge port of upstream 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, the access port that is equipped with variable valve on described carrier pipe and the described pneumatic tube and introduces fluidized gas;

Preferably, the internal surface of described container body is provided with wear-resisting and adiabatic lining.

Preferably, a plurality of described container bodys are arranged or along continuous straight runs is arranged or mix with horizontal direction along the vertical direction and arrange along the vertical direction.

Preferably, the fluidized gas supplied with of described fluidisation source of the gas is at least a in steam, oxygen, synthetic gas, the carbonic acid gas.

Preferably, described feed coal with send into described chopped-off head vaporizer after benzene class I liquid I material mixes, 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 the described container body is 1.0-9.0MPa.

Description of drawings

Fig. 1 is the synoptic diagram of high-pressure multi-stage fluidized-bed reactor according to an embodiment of the invention.

Fig. 2 is the synoptic 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 a plurality ofcontainer bodys 100 that order arranges, and is formed with vaporizer in eachcontainer body 100, and vaporizer is used for forming fluidized-bed within it.Preferably,container body 100 is preferably obround vessel, and the internal surface ofcontainer 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 opposite between a plurality ofcontainer bodys 100, what be positioned at the front container body is the upstream container body, the container body that is positioned at the back is the downstream reservoir body, for example be positioned at thetop container body 100 that links to each other with the feed coal source and can be called the chopped-off head container body, vaporizer in the chopped-off head container body can be called the chopped-off head vaporizer, fluidized-bed in the chopped-off head vaporizer can be called the chopped-off head fluidized-bed, be positioned at therearmost container body 100 that links to each other with the fluidisation source of the gas and can be called the final stage container body, vaporizer in the final stage container body can be called the final stage vaporizer, fluidized-bed in the final stage vaporizer can be called the final stage fluidized-bed, therefore, along the direction from the chopped-off head container body to the final stage container body, one side of contiguous chopped-off head container body is the upstream, and a side of contiguous final stage container body is the downstream.

In specific embodiments of the invention, a plurality ofcontainer 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.The final stage vaporizer also has the inlet for fluidization air that links to each other with fluidisation source of thegas 400, and the fluidized gas that fluidisation source of thegas 400 is supplied with can be at least a in steam, oxygen (pure oxygen, oxygen-rich air, air), synthetic gas and the carbonic acid gas.In adjacent two vaporizers, the inlet mouth that is positioned at the vaporizer of upstream links to each other by the pneumatic tube that is positioned atcontainer body 100 outsides with the air outlet of the vaporizer that is positioned at the downstream, and the discharge port that is positioned at the vaporizer of upstream links to each other by the carrier pipe that is positioned at described container body outside with the opening for feed of the vaporizer that is positioned at the 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, the access port that is equipped withvariable valve 500 on described carrier pipe and the described pneumatic tube and introduces fluidized gas is convenient to the adjusting of material and gas.

The inlet mouth of final stage vaporizer links to each other with vaporizedchemical source 300, and the opening for feed of chopped-off head vaporizer links to each other with the feed coal source by high-pressure oil coal slurry pump or high pressure coal dust pump.The discharge port of final stage vaporizer is used 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 with send into described chopped-off head vaporizer after benzene class I liquid I material mixes, described benzene class I liquid I material can be the by product according to the described high-pressure multi-stage fluidized-bed reactor of the embodiment of the invention.

In some embodiments of the invention, the gasification operation pressure in the high-pressure multi-stage fluidized-bed reactor can be compared with traditional fluidized-bed reactor in the scope of 1.0-9.0MPa, and pressure can improve greatly.In an embodiment of the present invention, " high pressure " can be the pressure greater than 1.0MPa.

High-pressure multi-stage fluidized-bed reactor according to the embodiment of the invention, comprise a plurality ofcontainer bodys 100, be positioned atcontainer body 100 outsides for the carrier pipe of material conveying betweencontainer body 100 and the pneumatic tube of delivering gas, can not cause disadvantageous effect to the fluidized-bed in the vaporizer in thecontainer body 100, and, because carrier pipe and pneumatic tube are positioned atcontainer body 100 outsides, can not bear the high temperature in the vaporizer, reduced the requirement to the material of carrier pipe and pneumatic tube, reduced cost, and replacing and easy to maintenance.In addition because a plurality ofcontainer bodys 100 series arrangement independently of one another, therefore, can according to arts demand along the vertical direction, horizontal direction or mix with horizontal direction up and down and arrange container body 100.Here, along up and down and horizontal direction mix arrangement, refer to the vertical central axis alignment of a part ofcontainer body 100, the vertical central axis of anotherpart 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 ofcontainer body 100 and the central axis of anotherpart 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 invention, gas-solid separator 200 has theinlet mouth 201 thatair outlet 202, semicoke returningcharge outlet 203 link to each other with air outlet with the chopped-off head vaporizer.Also be provided with on the sidewall of final stage vaporizer and the semicoke returningcharge outlet 203 semicoke opening for feeds that link to each other, the semicoke opening for feed of final stage vaporizer links to each other with fluidisation source of thegas 400 and is transported in the final stage vaporizer with the semicoke returning charge that will come from semicoke returningcharge outlet 203 by fluidized gas.

Preferably, be provided with the feed coal nozzle that stretches in the chopped-off head vaporizer in the opening for feed of chopped-off head vaporizer, be provided with the gas distributor that extend in this vaporizer in the inlet mouth of each vaporizer, be provided with the fluidized gas sparger that extend in the described final stage vaporizer in the inlet for fluidization air 119.The feed coal nozzle is a plurality of and evenly distributes 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 links to each other with vaporizedchemical 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 each vaporizer between chopped-off head vaporizer and the 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 all links to each other with fluidisation source of thegas 400 with the semicoke mass transport that will send from the vaporizer discharge port of upstream by fluidized gas in the vaporizer in adjacent downstream.

In a preferred embodiment of the invention, be equipped with the access port that variable valve and introducing fluidized gas enter on carrier pipe and the pneumatic tube.

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, the high-pressure multi-stage fluidized-bed reactor comprises fourcontainer bodys 100, that is: chopped-off head container body, second stage container body, third stage container body and final stage container body.Be formed with in the chopped-off head container body in the chopped-off head vaporizer A(chopped-off head vaporizer A and be formed with the chopped-off head fluidized-bed, in description of the invention, term " vaporizer " can exchange use with " fluidized-bed "), be formed with in the container body of the second stage in the vaporizer of the vaporizer B(second stage, the second stage and be formed with second stage fluidized-bed), be formed with in the third stage container body in the third stage vaporizer C(third stage vaporizer and be formed with third stage fluidized-bed), be formed with in the final stage level container body in the final stage vaporizer D(final stage vaporizer and be formed with the 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 the vertical central axis of chopped-off head container body and final stage container body is spaced apart in the horizontal direction.

In other words, form four vaporizer A-D of series arrangement in fourcontainer bodys 100, form the chopped-off head fluidized-bed respectively in four vaporizers, second stage fluidized-bed, third stage fluidized-bed and final stage fluidized-bed.

The upper portion side wall of chopped-off head vaporizer (also can be called the chopped-off head fluidized-bed) A is provided with chopped-off head fluidized-bed opening forfeed 102, be provided with feed coal nozzle 130 in the chopped-off head fluidized-bed opening forfeed 102, 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 the chopped-off head vaporizer A by feed coal nozzle 130, can improve gasification result thus.More preferably, feed coal nozzle 130 can further improve gasification result thus for a plurality of and evenly distribute along the circumferential interval of chopped-off head vaporizer A.

The roof of chopped-off head vaporizer A is provided with thesyngas outlet 101 on the vertical central axis that is positioned atcontainer body 100, the gas that produces in the chopped-off head vaporizer A can be discharged chopped-off head vaporizer A bysyngas outlet 101, because syngasoutlet 101 is positioned on the vertical central axis ofcontainer body 100, therefore, the discharging of synthetic gas is more smooth and easy, and there is not disadvantageous effect in the fluidized-bed in the vaporizers at different levels.The lower sides of chopped-off head vaporizer A is provided with chopped-off head fluidized-bed discharge port 104, and the material in the chopped-off head vaporizer A is discharged from chopped-off head fluidized-bed discharge port 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, thesecond stage 105, the sidewall of second stage vaporizer B is provided with second stage fluidized-bed opening forfeed 106, the sidewall of second stage vaporizer B is provided with the second stage fluidized-bed inlet mouth 107 that is communicated with the third stage fluidized-bed air outlet 109 of third stage vaporizer C by the pneumatic tube that is positioned atcontainer body 100 outsides, pneumatic tube is provided withvariable valve 500 and is used for introducing the access port that fluidized gas enters, gas in the 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 fluidized-bed discharge port 108, and the material in the vaporizer B of the second stage is discharged from second stage fluidized-bed discharge port 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 atcontainer body 100 outsides and being provided with the third stage fluidized-bed inlet mouth 113 that the pneumatic tube ofvariable valve 500 is communicated with the final stage fluidized-bed air outlet 114 of final stage vaporizer D, gas in the 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 the third stage vaporizer C forms and the generation of synthetic gas.The sidewall of third stage vaporizer C is provided with third stage fluidized-bed discharge port 111 and third stage fluidized-bed opening forfeed 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 forfeed 115, the sidewall of final stage vaporizer D is provided with final stage fluidized-bed opening forfeed 116, the lower sides of final stage fluidized-bed is provided with final stage fluidized-bed inlet mouth (linking to each other with liquid agent source 300) 118, final stage fluidized-bed discharge port (being grey slag notch) 117 and the inlet forfluidization air 119 that is used for linking to each other with fluidisation source of thegas 400, final stage fluidized-bed opening forfeed 116 is communicated with by the carrier pipe that is positioned atcontainer body 100 outsides with third stage fluidized-bed discharge port 111, and carrier pipe is provided withvariable valve 500 and introduces the access port that fluidized gas enters.Preferably,grey slag notch 117 is arranged in the lower sidewall of finalstage container body 100, the discharge of the lime-ash of being more convenient for thus.

Final stage fluidized-bed inlet mouth 118 links to each other with vaporizedchemical source 300, is used for supplying with vaporized chemical in final stage vaporizer D.Inlet forfluidization air 119 links to each other with fluidisation source of thegas 400, for supply flow gasification in final stage vaporizer D.

In vaporizedchemical import 118, be provided with the vaporized chemical sparger, in inlet forfluidization air 119, be provided with fluidizedgas sparger 119, so that the fluidized-bed in the 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 forfluidization 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 thepore 120 that is communicated with final stage vaporizer D.

Preferably, second stage fluidized-bed opening forfeed 106 links to each other with fluidisation source of thegas 400, and the semicoke mass transport that can will discharge from chopped-off head fluidized-bed discharge port 104 by fluidized gas is in the vaporizer B of the second stage thus.Third stage fluidized-bed opening forfeed 112 links to each other with fluidisation source of thegas 400, and the semicoke mass transport that can will go out from second stage fluidized-bed discharge port 108 by fluidized gas is in third stage vaporizer C thus; Final stage fluidized-bed opening forfeed 116 links to each other with fluidisation source of thegas 400 with the semicoke mass transport that will go out from third stage fluidized-bed discharge port 111 by fluidized gas in final stage vaporizer D.

In a preferred embodiment of the invention, the high-pressure multi-stage fluidized-bed reactor also comprises gas-solid separator 200, and gas-solid separator 200 has inletmouth 201,air outlet 202 and the semicoke returningcharge outlet 203 that is communicated with thesyngas outlet 101 of chopped-off head vaporizer A.

Also be provided with on the sidewall of final stage vaporizer D and the semicoke returningcharge outlet 203 semicoke returningcharge imports 115 that link to each other, semicoke returningcharge import 115 links to each other with fluidisation source of thegas 400 andexports 203 semicoke mass transport in final stage vaporizer D will come from the semicoke returning charge by fluidized gas.

Thus, enter gas-solid separator 200 from chopped-offhead container body 100 interior synthetic gas of discharging and carry out gas solid separation, the returning charge of isolated solid semicoke is discharged from semicoke returningcharge outlet 203, be transported in the final stage fluidized-bed D by fluidized gas by semicoke returningcharge import 115, improved utilization of materials, reduced and pollute.

High-pressure multi-stage fluidized-bed reactor according to the embodiment of the invention, vaporized chemical and fluidized gas are along upstream direction flows from the downstream, material is along downstream direction flows from the upstream, and material is carried by the carrier pipe that is positioned atcontainer body 100 outsides, gas is carried by the pneumatic tube that is positioned atcontainer body 100 outsides, there are not carrier pipe and pneumatic tube in thecontainer body 100, can not influence the fluidisation of the fluidized-bed in the vaporizers at different levels, reduced the requirement to carrier pipe and pneumatic tube material, reduced cost, be convenient to safeguard and change.

According to the high-pressure multi-stage fluidized-bed reactor of the embodiment of the invention, have H2, CH4 content height, gasification efficiency and the high characteristics of efficiency of carbon conversion in the synthetic gas.

High-pressure multi-stage fluidized-bed reactor according to the embodiment of the invention, coal dust or benzene class coal oil mixture material spray into chopped-off head vaporizer A by the pump pressurization by the nozzle on container body top, in the process that material descends, synthetic air rises to the first fluidized bed dryer section in the chopped-off head vaporizer A, and material is carried out preheating, drying, destructive distillation.Semicoke after the preheating by enter in the vaporizer B of the second stage second fluidized-bed and with the synthesis gas reaction of hydrogen rich gas, semicoke is converted to the synthetic gas that is rich in methane.Semicoke in the vaporizer B of the second stage after the gasification enters in the 3rd fluidized-bed in the third stage vaporizer C, and react with synthesis gas from the final stage fluidized-bed in the final stage vaporizer D, at the 3rd vaporizer, the carbon reaction in steam and the material semicoke generates the synthetic gas that H2, CO etc. are rich in methane.Semicoke after the 3rd vaporizer gasification enters in the final stage vaporizer, and is the synthetic gas of H2 and CO with generating major ingredient from the steam-oxygen (for example, pure oxygen, oxygen-rich air, air) of downstream vaporizer down with the carbon reaction.Thus, coal dust or benzene class slurry are after entering high-pressure multi-stage fluidized-bed reactor elder generation and steam-oxygen reaction, repeatedly fully contact with synthetic gas again and react, improved heat transfer rate, prolonged the residence time of pulverized coal particle in vapourizing furnace, improve the H2 in the synthetic gas, CH4 content height, thereby significantly improved efficiency of carbon conversion.

High-pressure multi-stage fluidized-bed reactor according to the embodiment of the 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 the synthetic gas can reach more than 15%, H2 content can reach more than 35%, have 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, compare with embodiment shown in Figure 1, difference is that fourcontainer bodys 100 arrange along the vertical direction, and the vertical central axis of fourcontainer bodys 100 overlaps each other.High-pressure multi-stage fluidized-bed reactor embodiment illustrated in fig. 2 and other structures of high-pressure multi-stage fluidized-bed reactor shown in Figure 1 and class of operation seemingly are not described in detail here.

High-pressure multi-stage fluidized-bed reactor according to the embodiment of the invention has the following advantages, 1) by adopting the nozzle ejection material, strengthened the mixed effect of semicoke and hydrogen-rich synthetic gas in the vaporizer, mass transfer, rate of heat transfer height effectively reduce the content of combustiblematerials in the lime-ash; 2) Qi Hua material flows in a plurality of vaporizers, H2, CO, CH4 in the gas forming amount height of unit mass coal dust, the effective gas, wherein efficiency of carbon conversion is up to more than 95%, CH4 content in the 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 are communicated with by carrier pipe and the pneumatic tube (for example riser tube, tremie pipe, scum pipe, air inlet and escape pipe) that is positioned at the container body outside, and the internal surface of pipe is provided with wear-resisting and adiabatic lining, prolonged the work-ing life of material pipeline, convenient maintenance has improved the online rate of installing; 4) reactor is simple in structure, the reliability height, and stable, production capacity is big, 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 many modification can be arranged.

Claims (14)

1. a high-pressure multi-stage fluidized-bed reactor is characterized in that, comprises a plurality of container bodys that order arranges, and has 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 also is provided with the inlet for fluidization air that links to each other with the fluidisation source of the gas; In adjacent two vaporizers, the inlet mouth that is positioned at the vaporizer of upstream links to each other by the pneumatic tube that is positioned at described container body outside with the air outlet of the vaporizer that is positioned at the downstream, the discharge port that is positioned at the vaporizer of upstream links to each other by the carrier pipe that is positioned at described container body outside with the opening for feed of the vaporizer that is positioned at the downstream, the opening for feed that wherein is positioned at the chopped-off head vaporizer of upstream links to each other with the 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 links to each other with the vaporized chemical source.

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 the inlet mouth that air outlet, semicoke returning charge outlet links to each other with air outlet with described chopped-off head vaporizer; Also be provided with the semicoke opening for feed that links to each other with described semicoke returning charge outlet on the sidewall of described final stage vaporizer, the semicoke opening for feed of described final stage vaporizer links to each other with described fluidisation source of the gas and is transported in the described final stage vaporizer with the semicoke returning charge that will come from described semicoke returning charge outlet by fluidized gas.

3. high-pressure multi-stage fluidized-bed reactor according to claim 1, it is characterized in that, be provided with the feed coal nozzle that stretches in the described chopped-off head vaporizer in the opening for feed of described chopped-off head vaporizer, be provided with the gas distributor that extend in this vaporizer in the inlet mouth of described vaporizer, be provided with the fluidized gas sparger that extend in the described final stage vaporizer in the described inlet for fluidization air.

4. high-pressure multi-stage fluidized-bed reactor according to claim 3 is characterized in that, described feed coal nozzle is a plurality of and evenly distributes along the circumferential interval of described chopped-off head vaporizer.

5. high-pressure multi-stage fluidized-bed reactor according to claim 1, it is characterized in that, the lower isolation of described final stage vaporizer goes out the fluidisation air chamber, the inlet mouth of described final stage vaporizer links to each other 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 each vaporizer between described chopped-off head vaporizer and the described final stage vaporizer is arranged on the top or sidewall of this vaporizer.

6. high-pressure multi-stage fluidized-bed reactor according to claim 1, it is characterized in that, except described chopped-off head vaporizer, the opening for feed of all the other all vaporizers all links to each other with described fluidisation source of the gas with the semicoke mass transport that will send from the vaporizer discharge port of upstream by fluidized gas in the vaporizer in adjacent downstream.

7. 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.

8. 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.

9. high-pressure multi-stage fluidized-bed reactor according to claim 8 is characterized in that, is equipped with variable valve on described carrier pipe and the described pneumatic tube and introduces the access port that fluidized gas enters.

10. 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.

11., it is characterized in that a plurality of described container bodys are arranged along the vertical direction or along continuous straight runs is arranged or along up and down and the arrangement of horizontal direction mixing according to each described high-pressure multi-stage fluidized-bed reactor among the claim 1-10.

12. 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 a in steam, oxygen, synthetic gas and the carbonic acid gas.

13. high-pressure multi-stage fluidized-bed reactor according to claim 1 is characterized in that, described feed coal with send into described chopped-off head vaporizer after benzene class I liquid I material mixes, described benzene class I liquid I material is the by product of described high-pressure multi-stage fluidized-bed reactor.

14. high-pressure multi-stage fluidized-bed reactor according to claim 1 is characterized in that, the gasification operation pressure in the described container body is 1.0-9.0MPa.

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