CN117304984A - Molten iron bath gasification furnace system with lead-bismuth liquid cyclone pyrolysis furnace arranged in front - Google Patents
Molten iron bath gasification furnace system with lead-bismuth liquid cyclone pyrolysis furnace arranged in front Download PDFInfo
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- CN117304984A CN117304984A CN202210943784.6A CN202210943784A CN117304984A CN 117304984 A CN117304984 A CN 117304984A CN 202210943784 A CN202210943784 A CN 202210943784A CN 117304984 A CN117304984 A CN 117304984A
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 288
- 239000007788 liquid Substances 0.000 title claims abstract description 186
- 229910052797 bismuth Inorganic materials 0.000 title claims abstract description 132
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 title claims abstract description 74
- 238000002309 gasification Methods 0.000 title claims abstract description 50
- 229910052742 iron Inorganic materials 0.000 title claims abstract description 37
- JCXGWMGPZLAOME-UHFFFAOYSA-N bismuth atom Chemical compound [Bi] JCXGWMGPZLAOME-UHFFFAOYSA-N 0.000 claims abstract description 86
- 230000007246 mechanism Effects 0.000 claims abstract description 68
- 238000003756 stirring Methods 0.000 claims abstract description 52
- 239000002910 solid waste Substances 0.000 claims abstract description 31
- 238000007667 floating Methods 0.000 claims abstract description 16
- 239000007789 gas Substances 0.000 claims description 191
- 239000000428 dust Substances 0.000 claims description 47
- 230000015572 biosynthetic process Effects 0.000 claims description 36
- 238000003786 synthesis reaction Methods 0.000 claims description 36
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 27
- 239000011261 inert gas Substances 0.000 claims description 23
- 238000001035 drying Methods 0.000 claims description 22
- 238000001816 cooling Methods 0.000 claims description 21
- 238000010438 heat treatment Methods 0.000 claims description 21
- 238000009833 condensation Methods 0.000 claims description 18
- 230000005494 condensation Effects 0.000 claims description 18
- 238000011084 recovery Methods 0.000 claims description 14
- 238000007599 discharging Methods 0.000 claims description 13
- 238000007598 dipping method Methods 0.000 claims description 12
- 230000007704 transition Effects 0.000 claims description 12
- 239000007921 spray Substances 0.000 claims description 11
- 238000005470 impregnation Methods 0.000 claims description 8
- 238000005192 partition Methods 0.000 claims description 8
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 6
- 238000001704 evaporation Methods 0.000 claims description 6
- 230000008020 evaporation Effects 0.000 claims description 6
- 238000011049 filling Methods 0.000 claims description 6
- 239000003546 flue gas Substances 0.000 claims description 6
- 238000004064 recycling Methods 0.000 claims description 5
- 238000005507 spraying Methods 0.000 claims description 5
- 239000000203 mixture Substances 0.000 claims description 4
- 238000001914 filtration Methods 0.000 claims description 3
- WABPQHHGFIMREM-UHFFFAOYSA-N lead(0) Chemical compound [Pb] WABPQHHGFIMREM-UHFFFAOYSA-N 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 12
- 230000008569 process Effects 0.000 abstract description 9
- 239000007787 solid Substances 0.000 abstract description 6
- 238000004227 thermal cracking Methods 0.000 abstract 1
- 235000019198 oils Nutrition 0.000 description 22
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 10
- 239000000463 material Substances 0.000 description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 5
- 239000000126 substance Substances 0.000 description 4
- 230000009471 action Effects 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 239000002296 pyrolytic carbon Substances 0.000 description 3
- 230000033764 rhythmic process Effects 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000007664 blowing Methods 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 239000007790 solid phase Substances 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- 239000008346 aqueous phase Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000012840 feeding operation Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 235000019476 oil-water mixture Nutrition 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 239000012716 precipitator Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/57—Gasification using molten salts or metals
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention relates to a molten iron bath gasification furnace system with a front lead bismuth liquid cyclone pyrolysis furnace, which comprises the following steps: the molten lead bismuth liquid circulation tank is internally provided with molten lead bismuth liquid and a stirring mechanism, the added organic solid waste is subjected to centrifugal rotational flow along with the molten lead bismuth liquid and simultaneously subjected to thermal cracking, pyrolysis gas escapes, is collected, condensed and pressurized and then enters the molten iron bath gasification furnace, and pyrolysis residual solids floating on the lead bismuth liquid are lifted in the rotational flow process and enter molten iron liquid contained in the molten pool gasification furnace for further pyrolysis gasification. The invention can realize high-efficiency pyrolysis, so that the front pyrolysis link is matched with the final molten pool type gasification.
Description
Technical Field
The invention relates to the technical field of energy, in particular to a molten iron bath gasification furnace system with a front lead-bismuth liquid cyclone pyrolysis furnace.
Background
When solid waste is gasified by the molten iron bath, the solid phase, pyrolysis liquid and non-condensable gas obtained by pyrolysis of the organic solid waste are respectively input into a molten pool gasifier for final stable conversion into synthesis gas after the organic solid waste is subjected to medium-temperature pyrolysis due to the fact that physical properties of the solid waste are quite different and chemical components are quite fluctuating.
At present, the conventional pyrolysis process and pyrolysis furnace adopt an indirect heating means of solid phase heat conduction, the pyrolysis time of organic solid waste is 40-400 minutes, the gasification process of the high-efficiency molten pool gasification furnace is less than 1 second, and the pre-working procedure can not meet the requirement of the main process. Hundred-ton-level material gasification can be realized by a single gasification furnace per hour, and a conventional pyrolysis furnace only has ton-level per hour, so that the rhythm and the productivity of the pyrolysis furnace are seriously mismatched.
Therefore, a leading pyrolysis system of liquid phase heat transfer is needed, and the system of the molten iron bath gasification furnace with the leading lead bismuth liquid cyclone pyrolysis furnace is adopted in the application, so that the problems that the rhythm of the pyrolysis furnace is too slow, the productivity is too small, and the leading pyrolysis and the final gasification are seriously mismatched at present are solved.
Disclosure of Invention
The invention aims to solve the problems in the prior art and provides a molten iron bath gasification furnace system with a lead-bismuth liquid cyclone pyrolysis furnace arranged in front.
In order to achieve the above object, the present invention adopts the following technical scheme: the molten iron bath gasification furnace system with the lead-bismuth liquid cyclone pyrolysis furnace comprises:
the lead-bismuth liquid circulation tank is internally provided with molten lead-bismuth liquid and a stirring mechanism for stirring the lead-bismuth liquid to form centrifugal rotational flow;
the feeding mechanism is used for sending the organic solid waste into the lead-bismuth liquid circulation tank for pyrolysis to generate pyrolysis gas;
the pyrolysis gas recovery mechanism is communicated with the pyrolysis gas outlet of the lead bismuth liquid circulation pool and is partially arranged outside the feeding mechanism, and is used for storing the pyrolysis gas to the pyrolysis gas temporary storage chamber and realizing the preheating of organic solid waste through the heat exchange between the pyrolysis gas and the outer wall of the feeding mechanism;
the pyrolysis gas condensation recovery mechanism is communicated with the pyrolysis gas temporary storage chamber and is used for converging and pressurizing part of pyrolysis liquid after first condensation in the pyrolysis gas temporary storage chamber and then spraying the part of pyrolysis liquid into the molten pool gasifier, and the rest part of pyrolysis gas is subjected to secondary condensation, converging, standing and layering for storage and recovery utilization respectively;
the lead bismuth liquid standing pool is communicated with the lead bismuth liquid circulation pool and is provided with a discharge mechanism for lifting and discharging pyrolysis residues floating on the surface of the lead bismuth liquid circulation pool;
a gasification furnace feed hopper for receiving pyrolysis residues discharged by the discharge mechanism and pressurizing and feeding the pyrolysis residues into a molten pool gasification furnace;
the molten pool gasifier is communicated with a gasifier feed hopper through an impregnation feeding upper pipe and an impregnation feeding lower pipe, and is internally provided with a molten iron bath pool containing molten iron liquid, and is used for immersing pyrolysis residues, pyrolysis liquid and pyrolysis non-condensable gas into the molten iron bath pool to realize thorough pyrolysis-gasification, so as to obtain synthesis gas, and the synthesis gas is discharged through a synthesis gas channel;
the synthesis gas cooling treatment mechanism is communicated with the synthesis gas channel and is used for cooling the synthesis gas for a plurality of times, respectively storing the cooled synthesis gas, and finally filtering and dedusting the cooled synthesis gas to output clean normal-temperature synthesis gas;
the heating chamber of the lead bismuth liquid pool is provided with a hot air inlet and a hot air outlet which are used for indirectly heating the lead bismuth liquid circulation pool and the lead bismuth liquid standing pool.
Working principle and beneficial effect: 1. compared with the prior art, the method has the advantages that the low-melting-point molten alloy lead-bismuth liquid is used as a heat carrier, organic solid waste is added into the rotational flow lead-bismuth liquid which is molten at about 500 ℃ to be subjected to rapid pyrolysis, pyrolysis residual solids float on the surface of the lead-bismuth liquid, the pyrolysis residual solids are hermetically sent into a molten pool gasifier to be subjected to pyrolysis-gasification by adopting a spiral lifting conveying mechanism, so that the organic solid waste takes 10-30 seconds from the addition to the completion of medium-temperature pyrolysis, and the pyrolysis time is greatly shortened compared with the original 40-400 minutes. The method is beneficial to the direct contact between the lead bismuth liquid and the organic solid waste, and the accumulation amount of the lead bismuth liquid and the organic solid waste added in unit time can be flexibly adjusted through convection heat exchange, so that the pyrolysis efficiency is greatly improved;
2. compared with the prior art, the pyrolysis residual solids in the treatment process can be directly hot charged into the molten pool gasifier, so that the heat loss is reduced, large-scale pretreatment can be realized through a single pyrolysis furnace, and the molten pool gasifier with the solid waste gasification amount of 50-150 tons per hour of the single pyrolysis furnace can be orderly connected and matched.
Further, pyrolysis gas recovery mechanism is including locating the pyrolysis gas flue of feeding mechanism outside and with lead bismuth liquid circulation pond's pyrolysis gas export intercommunication, be used for prolonging pyrolysis gas discharge route, increase the flue gas baffling board of heat exchange time and be used for the stoving gas channel of discharge stoving gas, pyrolysis gas flue top intercommunication pyrolysis gas temporary storage room, pyrolysis gas recovery mechanism still is used for carrying out heat transfer with pyrolysis gas discharge through feeding mechanism outer wall to make the organic solid waste in the feeding mechanism preheated.
The device can effectively utilize the heat of the pyrolysis gas, thereby obviously reducing the heat loss, and simultaneously, the device can fully heat to maintain the constant temperature of the lead bismuth liquid and reduce the use of external energy.
Further, the feeding mechanism comprises a feeding bin, a spiral feeding pipe communicated with the feeding bin, a first spiral arranged in the spiral feeding pipe, a plurality of heat exchange fins arranged on the outer wall of the spiral feeding pipe and a drying gas collecting pipe for collecting the escaped organic solid waste heated and evaporated moisture, wherein the drying gas collecting pipe is communicated with a drying gas channel, and a plurality of moisture evaporation holes communicated with the drying gas collecting pipe are formed in the spiral feeding pipe.
The device can effectively evaporate the water in the organic solid waste, and also realizes preliminary preheating of the organic solid waste in the feeding process.
Further, the pyrolysis gas condensation recovery mechanism comprises a pyrolysis oil condenser for condensing pyrolysis gas discharged from the pyrolysis gas temporary storage chamber for the first time, a pyrolysis oil pressurizing pump for pressurizing pyrolysis liquid, a pyrolysis liquid spray pipe for adding the pressurized pyrolysis liquid into the dipping feeding lower pipe, a pyrolysis mixed liquid condenser for condensing pyrolysis gas for the second time, a pyrolysis non-condensable gas booster pump for pressurizing residual pyrolysis gas and a pyrolysis non-condensable gas storage tank for storing the pressurized residual pyrolysis gas, wherein the pyrolysis non-condensable gas storage tank is used for adding the residual pyrolysis gas into the molten pool gasifier through a non-condensable gas spray pipe.
The device can effectively recycle the pyrolysis gas, separate the condensable part and the non-condensable part in the pyrolysis gas for separate storage and temporary storage, and then add the pyrolysis gas into the molten pool gasifier, so that the gasification efficiency can be obviously improved, and the rhythm of the pyrolysis furnace can be matched with that of the upper molten pool gasifier.
Further, the pyrolysis mixed liquid condenser is also used for collecting the mixture of the pyrolysis liquid and water after secondary condensation, standing and layering, sending the pyrolysis liquid on the upper layer into a pyrolysis mixed liquid floating oil tank, pressurizing through a pyrolysis floating oil pressurizing pump, adding the pyrolysis liquid into a dipping feeding lower pipe through a pyrolysis oil spray pipe, sending the water phase part on the lower layer into a pyrolysis condensation water tank, and processing the pyrolysis liquid into cyclic utilization through a water treatment unit.
Further, be equipped with the division wall on the lead bismuth liquid pond of standing, be equipped with a plurality of access holes on this division wall, so that lead bismuth liquid can pass through and block pyrolysis residue, and discharge mechanism is including the pyrolysis residue spiral riser that the slope set up, locate the second spiral in this pyrolysis residue spiral riser and locate a plurality of weeping holes on this pyrolysis residue spiral riser, promote the discharge with pyrolysis residue through the second spiral, retrieve the lead bismuth liquid that the pyrolysis residue was carried to the lead bismuth liquid in the pond of standing through weeping hole.
Further, the stirring mechanism comprises a stirring impeller arranged in the lead bismuth liquid circulation pool and a stirring motor used for driving the stirring impeller, and the stirring motor is positioned outside the lead bismuth liquid circulation pool and connected with the stirring impeller through a stirring shaft.
Further, a plurality of hot air baffles are arranged in the heating chamber of the lead bismuth liquid pool so as to prolong the hot air flow path and increase the heat exchange time and the heat exchange area.
Further, the top of the gasification furnace feed hopper is provided with a pyrolysis residue transition chamber, a second locking bucket valve is arranged between the pyrolysis residue transition chamber and the gasification furnace feed hopper, the gasification furnace feed hopper is also connected with a second vacuum pump and a second high-pressure inert gas tank, the second vacuum pump is used for vacuumizing the gasification furnace feed hopper through a second air suction port, the second high-pressure inert gas tank is used for filling inert gas into the gasification furnace feed hopper through a second air charging valve and an air charging port positioned on the gasification furnace feed hopper, and a second lower locking bucket valve is arranged between the bottom of the gasification furnace feed hopper and the upper dipping feeding pipe.
Further, the synthetic gas cooling treatment mechanism comprises a cold dust chamber, a second cold dust chamber and a final cold dust collector which are sequentially arranged along the advancing direction of the synthetic gas, wherein a first lock hopper valve and a cold ash carrying tank are arranged at the bottom of the cold dust chamber, a second lock hopper valve and a second cold ash carrying tank are arranged at the bottom of the second cold dust chamber, a third lock hopper valve and a final cold ash carrying tank are arranged at the bottom of the final cold dust collector, the final cold dust collector is used for discharging clean normal-temperature synthetic gas, and the first cold ash carrying tank, the second cold ash carrying tank and the second cold ash carrying tank are used for regularly collecting dust.
Further, the feeding mechanism comprises an upper lock hopper provided with an upper lock hopper valve, a first vacuum pump for vacuumizing the upper lock hopper through a first air suction port, a first high-pressure inert gas tank for filling inert gas into the upper lock hopper through a first air charging valve and a first air charging port, a lower lock hopper arranged below the upper lock hopper and a first lock hopper valve arranged between the upper lock hopper and the lower lock hopper, a spiral feeding pipe communicated with the center top of the lead bismuth liquid ring flow pool is arranged at the bottom of the lower lock hopper, a first spiral is arranged in the spiral feeding pipe, the bottom of the first spiral is connected with a stirring impeller of the stirring mechanism, and the stirring impeller is driven to rotate through the first spiral to simultaneously add organic solid waste into the lead bismuth liquid ring flow pool.
Drawings
FIG. 1 is a schematic diagram of a lead bismuth liquid cyclone pyrolysis furnace of the present invention;
FIG. 2 is a section A-A of FIG. 1;
fig. 3 is a partial top view of the lead bismuth liquid cyclone pyrolysis furnace of the present invention;
fig. 4 is a partial top view of another preferred lead bismuth liquid cyclone pyrolysis furnace;
fig. 5 is a partial left side view of the lead bismuth liquid cyclone pyrolysis furnace of the present invention;
FIG. 6 is a schematic diagram of pyrolysis gas condensation process and flow direction according to the present invention;
FIG. 7 is a schematic view of a molten bath gasifier according to the present invention;
FIG. 8 is a schematic view of another preferred stirring mechanism;
fig. 9 is a sectional view of B-B in fig. 8.
In the figure, 101, a feeding bin; 102. a screw feeding tube; 103. a first spiral; 104. a pyrolysis gas flue; 105. a drying gas passage; 106. a water evaporation hole; 107. a flue gas baffle; 108. a heat exchange fin; 109. a drying gas collecting pipe; 120. a pyrolysis gas temporary storage chamber; 121. a pyrolysis oil condenser; 122. a pyrolysis oil pressurizing pump; 123. a pyrolysis mixed liquor condenser; 124. pyrolyzing the mixed liquid floating oil tank; 125. a pyrolysis oil slick pressurizing pump; 126. pyrolysis condensed water tank; 127. a pyrolysis noncondensable gas booster pump; 128. a pyrolysis noncondensable gas storage tank; 130. a water treatment unit; 145. a first air suction port; 146. a first vacuum pump; 147. a first inflation port; 148. a first inflation valve; 149. a first high pressure inert gas tank; 151. locking a bucket; 152. a lower lock hopper; 153. a first lock hopper valve; 154. a first lock hopper valve; 201. a lead bismuth liquid circulation pool; 202. a lead bismuth liquid standing pool; 203. a heating chamber of a lead bismuth liquid pool; 204. lead bismuth liquid; 205. a stirring impeller; 206. a stirring shaft; 207. a stirring motor; 208. a partition wall; 209. a liquid through hole; 220. a hot air baffle; 221. a hot air inlet; 222. a hot air outlet; 301. pyrolyzing the residue; 302. a pyrolysis residue spiral riser; 303. a second helix; 304. a weeping hole; 401. a pyrolysis residue transition chamber; 402. a gasification furnace feed hopper; 403. a second lock hopper valve; 404. a second lower lock hopper valve; 405. an air suction port; 406. a second vacuum pump; 407. a second inflation port; 408. a second inflation valve; 409. a second high pressure inert gas tank; 501. dipping the feeding upper pipe; 502. dipping and feeding the material into a lower pipe; 503. a molten pool gasifier; 504. a molten iron bath; 505. an oxygen lance; 506. a pyrolysis liquid spray pipe; 507. a non-condensable gas spraying pipe; 508. a synthesis gas channel; 509. a cold dust removal chamber; 510. a first lock hopper valve; 511. a cold ash-bearing tank; 512. a secondary cooling dust removing chamber; 513. a second lock hopper valve; 514. a second cooling ash-bearing tank; 515. a final cooling dust remover; 516. a third lock hopper valve; 517. a final cooling ash-bearing tank; 518. a synthesis gas user.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which are derived by a person skilled in the art based on the embodiments of the invention, fall within the scope of protection of the invention.
It will be appreciated by those skilled in the art that in the present disclosure, the terms "longitudinal," "transverse," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," etc. refer to an orientation or positional relationship based on that shown in the drawings, which is merely for convenience of description and to simplify the description, and do not indicate or imply that the apparatus or elements referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore the above terms should not be construed as limiting the invention.
Example 1
As shown in fig. 1 to 7, the present molten iron bath gasification furnace system with a lead bismuth liquid front-end cyclone pyrolysis furnace comprises:
wherein, the lead bismuth liquid circulation pool 201 is internally provided with molten lead bismuth liquid 204 with the temperature of about 500 ℃ and a stirring mechanism for stirring the lead bismuth liquid 204 to form centrifugal rotational flow;
the stirring mechanism comprises a stirring impeller 205 arranged in the lead bismuth liquid circulation tank 201 and a stirring motor 207 for driving the stirring impeller 205, wherein the stirring motor 207 is positioned outside the lead bismuth liquid circulation tank 201 and is connected with the stirring impeller 205 through a stirring shaft 206;
wherein, the feeding mechanism is used for sending the organic solid waste into the lead bismuth liquid circulation pool 201 for pyrolysis to generate pyrolysis gas;
preferably, as shown in fig. 1 to 4, the feeding mechanism comprises a feeding bin 101, a screw feeding pipe 102 communicated with the feeding bin 101, a first screw 103 arranged in the screw feeding pipe 102, a plurality of heat exchange fins 108 arranged on the outer wall of the screw feeding pipe 102 and a drying gas collecting pipe 109 for collecting the water evaporated by heating of the escaping organic solid waste, wherein the drying gas collecting pipe 109 is communicated with a drying gas channel 105, and a plurality of water evaporation holes 106 communicated with the drying gas collecting pipe 109 are arranged on the screw feeding pipe 102.
In which the direction of the charging mechanism is different in fig. 3 and 4.
In another preferred embodiment, as shown in fig. 8 and 9, the feeding mechanism comprises an upper lock hopper 151 provided with an upper lock hopper 151 valve, a first vacuum pump 146 for evacuating the upper lock hopper 151 through a first suction port 145, a first high-pressure inert gas tank 149 for filling inert gas into the upper lock hopper 151 through a first inflation valve 148 and a first inflation port 147, a lower lock hopper 152 provided below the upper lock hopper 151, and a first lock hopper valve 510 provided between the upper lock hopper 151 and the lower lock hopper 152, a screw feeding pipe 102 communicated with the central top of the lead bismuth liquid circulation tank 201 is provided at the bottom of the lower lock hopper 152, a first screw 103 is provided in the screw feeding pipe 102, a stirring impeller 205 of the stirring mechanism is connected at the bottom of the first screw 103, and the stirring impeller 205 is driven to rotate through the first screw 103 while adding organic solid waste into the lead bismuth liquid circulation tank 201.
As shown in fig. 1 and 8, the pyrolysis gas recovery mechanism is communicated with the pyrolysis gas outlet of the lead-bismuth liquid circulation tank 201 and is partially arranged outside the feeding mechanism, and is used for storing the pyrolysis gas into the pyrolysis gas temporary storage chamber 120, and preheating organic solid waste through heat exchange between the pyrolysis gas and the outer wall of the feeding mechanism;
in this embodiment, the pyrolysis gas recovery mechanism includes the pyrolysis gas flue 104 that locates outside the charging mechanism and communicates with the pyrolysis gas outlet of plumbous bismuth liquid circulation pond 201, be used for prolonging pyrolysis gas discharge path, increase the flue gas baffling board 107 of heat exchange time and be used for discharging the stoving gas passageway 105, pyrolysis gas flue 104 top intercommunication pyrolysis gas temporary storage chamber 120, pyrolysis gas recovery mechanism still is used for discharging the pyrolysis gas through charging mechanism outer wall heat transfer to make the organic solid waste in the charging mechanism preheated.
The pyrolysis gas condensation recovery mechanism is communicated with the pyrolysis gas temporary storage chamber 120 and is used for converging and pressurizing part of pyrolysis liquid after first condensation in the pyrolysis gas temporary storage chamber 120 and then spraying the part of pyrolysis liquid into the molten pool gasifier 503, and the rest part of pyrolysis gas is secondarily condensed and converged, and is kept still and layered to be respectively stored and recycled;
in the present embodiment, the pyrolysis gas condensation recovery mechanism includes a pyrolysis oil condenser 121 for condensing the pyrolysis gas discharged from the pyrolysis gas temporary storage chamber 120 for the first time, a pyrolysis oil pressurizing pump 122 for pressurizing the pyrolysis liquid, a pyrolysis liquid nozzle 506 for adding the pressurized pyrolysis liquid to the impregnation-feed down pipe 502, a pyrolysis mixed liquid condenser 123 for condensing the pyrolysis gas for the second time, a pyrolysis non-condensable gas pressurizing pump 127 for pressurizing the remaining pyrolysis gas, and a pyrolysis non-condensable gas storage tank 128 for storing the pressurized remaining pyrolysis gas, the pyrolysis non-condensable gas storage tank 128 being to be fed through the non-condensable gas nozzle 507The residual pyrolysis gas is added into a molten pool gasifier 503, the temperature of molten iron liquid contained in a molten iron bath 504 in the molten pool gasifier 503 is 1350-1500 ℃, the immersed solid carbon, organic gas and organic liquid can be thoroughly pyrolyzed, and under the action of blowing oxygen, the organic matter is partially oxidized into CO/CO 2 And H 2 /H 2 O (water vapor) and inorganic inert substances are also in the molten state at this temperature.
Preferably, the pyrolysis mixed liquor condenser 123 is further used for collecting and standing and layering a mixture of the pyrolysis liquor and water after secondary condensation, sending the pyrolysis liquor at the upper layer to the pyrolysis mixed liquor floating oil tank 124, pressurizing the pyrolysis mixed liquor by the pyrolysis floating oil pressurizing pump 125, adding the pyrolysis liquor into the impregnation feeding lower pipe 502 by the pyrolysis oil spray pipe, sending the water phase part at the lower layer to the pyrolysis condensation water tank 126, and processing the water phase part by the water treatment unit 130 for recycling.
Wherein, the lead bismuth liquid standing pool 202 is communicated with the lead bismuth liquid circulation pool 201 and is provided with a discharge mechanism for lifting and discharging pyrolysis residues 301 floating on the surface of the lead bismuth liquid circulation pool 201;
in this embodiment, a partition wall 208 is disposed on the lead-bismuth liquid standing pool 202, a plurality of liquid through holes 209 are disposed on the partition wall 208, so that the lead-bismuth liquid 204 can pass through and block the pyrolysis residue 301, and the discharging mechanism includes a pyrolysis residue spiral riser 302 disposed obliquely, a second spiral 303 disposed in the pyrolysis residue spiral riser 302, and a plurality of liquid leakage holes 304 disposed on the pyrolysis residue spiral riser 302, the pyrolysis residue 301 is lifted and discharged through the second spiral 303, and the lead-bismuth liquid 204 entrained by the pyrolysis residue 301 is recovered into the lead-bismuth liquid standing pool 202 through the liquid leakage holes 304.
Wherein, the gasification furnace feed hopper 402 is used for receiving the pyrolysis residues 301 discharged by the discharge mechanism and pressurizing and feeding the pyrolysis residues into the molten pool gasification furnace 503;
preferably, a pyrolysis residue transition chamber 401 is arranged at the top of the gasifier feed hopper 402, a second upper lock hopper valve 403 is arranged between the pyrolysis residue transition chamber 401 and the gasifier feed hopper 402, the gasifier feed hopper 402 is also connected with a second vacuum pump 406 and a second high-pressure inert gas tank 409, the second vacuum pump 406 is used for vacuumizing the gasifier feed hopper 402 through a second air suction port 405, the second high-pressure inert gas tank 409 is used for filling inert gas into the gasifier feed hopper 402 through a second air charging valve 408 and an air charging port positioned on the gasifier feed hopper 402, and a second lower lock hopper valve 404 is arranged between the bottom of the gasifier feed hopper 402 and the impregnating upper charging pipe 501.
Wherein, the molten pool gasifier 503 is communicated with the gasifier feed hopper 402 through the upper dipping feeding pipe 501 and the lower dipping feeding pipe 502, and is internally provided with a molten iron bath pool 504 filled with molten iron liquid, and is used for immersing pyrolysis residues 301, pyrolysis liquid and pyrolysis noncondensable gas into the molten iron bath pool 504 to realize thorough pyrolysis-gasification, thus obtaining synthesis gas, and the synthesis gas is discharged through a synthesis gas channel 508;
the synthesis gas cooling treatment mechanism is communicated with the synthesis gas channel 508 and is used for respectively storing the cooled synthesis gas for a plurality of times, and finally filtering and dedusting the cooled synthesis gas to output clean normal-temperature synthesis gas to a synthesis gas user 518;
in this embodiment, the cooling treatment mechanism for the synthetic gas comprises a cold dust chamber 509, a second cold dust chamber 512 and a final cold dust collector 515 sequentially arranged along the proceeding direction of the synthetic gas, wherein a first lock valve 510 and a cold ash carrying tank 511 are arranged at the bottom of the cold dust chamber 509, a second lock valve 513 and a second cold ash carrying tank 514 are arranged at the bottom of the second cold dust chamber 512, a third lock valve 516 and a final cold ash carrying tank 517 are arranged at the bottom of the final cold dust collector 515, and the final cold dust collector 515 is used for discharging clean normal-temperature synthetic gas, and the first cold ash carrying tank 511, the second cold ash carrying tank 514 and the second cold ash carrying tank 514 are used for periodically collecting dust.
Wherein the lead bismuth liquid pool heating chamber 203 is provided with a hot air inlet 221 and a hot air outlet 222 for indirectly heating the lead bismuth liquid circulation pool 201 and the lead bismuth liquid standing pool 202.
Preferably, a plurality of hot air baffles 220 are provided within the lead bismuth pool heating chamber 203 to extend the hot air flow path, increase heat exchange time and heat exchange area.
Example two
The present embodiment is based on implementation one for illustrating the process flow of the present application.
As shown in fig. 1-7, in the first step, organic solid waste is added from a feeding bin 101, falls into a spiral feeding pipe 102, and is pushed downwards by a first spiral 103, and then moves downwards in the spiral feeding pipe 102, falls into a lead-bismuth liquid 204 of a lead-bismuth liquid circulation pool 201, the temperature of the lead-bismuth liquid is 500 ℃, and the lead-bismuth liquid 204 rotates at a certain angular speed under the rotary stirring action of a stirring impeller 205. The driving force for the rotation of the stirring impeller 205 is realized by a stirring motor 207 through a stirring shaft 206, and the upper part of the stirring shaft 206 and the stirring motor 207 are positioned outside the lead bismuth liquid circulation tank 201. The organic solid waste falling into the lead bismuth liquid pool is heated by the lead bismuth liquid to be pyrolyzed, pyrolysis gas moves outwards along the pyrolysis gas flue 104, is blocked by the flue gas baffle 107, contacts and exchanges heat with the pipe wall of the spiral feeding pipe 102 and the heat exchange fins 108 outside the pipe of the spiral feeding pipe 102, so that the organic solid waste added later is preheated, water is evaporated from the water evaporation holes 106, and is collected to the drying gas collecting pipe 109 and discharged from the drying gas channel 105. The pyrolysis gas enters the pyrolysis gas temporary storage chamber 120 from the pyrolysis gas flue 104 for temporary storage.
Step two, pyrolysis gas is condensed to 150 ℃ for the first time after passing through the pyrolysis gas temporary storage chamber 120, and the pyrolysis liquid is dripped and collected into the pyrolysis oil condenser 121, pressurized by the pyrolysis oil pressurizing pump 122, added into the dipping feeding lower pipe 502 through the pyrolysis liquid spray pipe 506, and enters into the deep part of the molten iron bath 504 of the molten bath gasifier 503; similarly, the secondary condensation temperature is 50 ℃, the pyrolysis liquid is an oil-water mixture, condensed and dripped and collected into the pyrolysis mixed liquid condenser 123, the mixture is kept stand and layered, the upper layer oil enters the pyrolysis mixed liquid floating oil tank 124, is pressurized by the pyrolysis floating oil pressurizing pump 125, and is sprayed into the dipping feeding lower pipe 502 of the molten pool gasification furnace through the pyrolysis liquid spray pipe 506 to be gasified. The stratified aqueous phase fraction passes from the pyrolysis condensate tank 126 to the water treatment unit 130. The pyrolysis gas is pressurized by a pyrolysis noncondensable gas booster pump 127 and enters a pyrolysis noncondensable gas storage tank 128, and then is added to a molten pool gasifier 503 through a noncondensable gas nozzle 507.
And thirdly, the pyrolysis residues 301 which are carbon residues and inorganic inert ash substances and remain in the lead-bismuth liquid circulation tank 201 float on the surface of the lead-bismuth liquid circulation tank 201, along with the rotational flow of the whole tank, enter into the lead-bismuth liquid standing tank 202, the rotational flow is blocked by the partition wall 208, the partition wall 208 is provided with a plurality of through liquid holes 209, so that the lead-bismuth liquid 204 can pass through, floating carbon residues are retained on one side of the surface of the lead-bismuth liquid standing tank 202 and are close to the lower port of the pyrolysis residue spiral riser 302, the floating carbon residues are driven to rise by the second spiral 303, the entrained lead-bismuth liquid is leaked through the liquid leakage holes 304, and finally the upper port of the pyrolysis residue spiral riser 302 falls into the pyrolysis residue transition chamber 401.
The lead bismuth liquid circulation tank 201 and the lead bismuth liquid standing tank 202 are both positioned in the lead bismuth liquid tank heating chamber 203, the lead bismuth liquid tank heating chamber 203 is provided with a hot air inlet 221 and a hot air outlet 222, hot air with the temperature higher than 500 ℃ enters from the hot air inlet 221, and indirectly transfers heat to the lead bismuth liquid through the outer walls of the lead bismuth liquid circulation tank 201 and the lead bismuth liquid standing tank 202 so as to supplement the heat absorbed by pyrolysis of organic matters and heating of materials, finally the hot air is discharged from the hot air outlet 222, a plurality of hot air baffle plates 220 are arranged in the lead bismuth liquid tank heating chamber 203 and welded on the outer walls of the lead bismuth liquid circulation tank 201 and the lead bismuth liquid standing tank 202, so that the hot air stays in the lead bismuth liquid tank heating chamber 203 for a long time, the heat exchange area is increased, and the lead bismuth liquid is sufficiently heated to maintain the temperature constant.
Step four, pyrolytic carbon residue enters into a pyrolytic residue transition chamber 401, a second upper lock hopper valve 403 is opened, pyrolytic carbon residue enters into a gasifier feed hopper 402, inert gas CO2 in a second high-pressure inert gas tank 409 enters into a second charging port 407 through an opened second charging valve 408, the gasifier feed hopper 402 is charged, after pressurization and impregnation feeding upper pipe 501 are balanced, a second lower lock hopper valve 404 is opened, so that carbon residue falls into the impregnation feeding upper pipe 501, then the second lower lock hopper valve 404 is rapidly closed, a second vacuum pump 406 is started to pump air through a second air suction port 405, so that the air pressure of the gasifier feed hopper 402 is reduced to be balanced with the pyrolytic residue transition chamber 401, and then the second upper lock hopper valve 403 is opened to accept pyrolytic carbon residue falling into the next pyrolytic residue transition chamber 401.
In the step five, in the molten pool gasifier 503, solid carbon slag falling from the upper impregnating and feeding pipe 501 falls onto the surface of the molten iron bath 504 through the lower impregnating and feeding pipe 502, oxygen is blown into the oxygen lance 505, a pyrolysis liquid spray pipe 506 is injected into the pyrolysis liquid, and a noncondensable gas spray pipe 507 is blown intoContinuously heating up pyrolysis-gasification of pressurized pyrolysis noncondensable gas in the cavity of the dipping feeding lower pipe 502, and finally washing by molten iron bath and slag liquid with the temperature of up to 1500 ℃ in a molten iron bath pool 504 to obtain CO and H 2 、CO 2 The high-temperature coarse synthesis gas composed of water vapor is discharged through the synthesis gas channel 508 and enters a cold dust removal chamber 509 for cooling and dust removal, dust removal ash is accumulated at the bottom of the cold dust removal chamber 509, and a first lock hopper valve 510 is opened periodically, so that cold dust blowing ash enters a cold dust bearing tank 511. The primarily purified and cooled synthesis gas continues to move along the pipeline, and is subjected to secondary cooling and dust removal in the secondary cooling and dust removal chamber 512, secondary dust removal ash drops to the bottom of the secondary cooling and dust removal chamber 512, and the second lock hopper valve 513 is opened periodically, so that the secondary dust removal ash drops to the secondary cooling and dust holding tank 514. After a third final cooling by the final cooling precipitator 515, the clean room temperature syngas is delivered to the syngas user 518. A small amount of dust discharged from the final-cooling dust remover 515 is periodically discharged to the final-cooling dust-holding tank 517 through the third lock valve 516.
In another embodiment of the feeding mechanism, as shown in fig. 8, the first screw 103 and the stirring impeller 205 are coaxially arranged, the lower end of the screw feeding tube 102 goes deep into the lead bismuth liquid, and then the first screw 103 and the lowest drying gas channel 105 which are not wrapped by the screw feeding tube 102 are arranged downwards. The first locking hopper valve 153 is opened, the material falls into the locking hopper 151, the first high-pressure inert gas tank 149 is pressurized to be higher than the gas pressure above the lead bismuth liquid 204 through the first gas charging valve 148 and the first gas charging port 147, then the first lower locking hopper valve 154 is opened, the material falls into the lower locking hopper 152, and the first lower locking hopper valve 154 is closed immediately after rotation. The material is rotated downwards under the action of the first screw 103, finally the screw feeding tube 102 is extruded at the lower end of the screw feeding tube 102, the material enters the lead bismuth liquid 204, pyrolysis occurs under heating, and simultaneously floats upwards, and the pyrolysis carbon residue is lifted off the lead bismuth liquid 204 by the second screw 303 along with the whole molten pool rotational flow on the surface of the lead bismuth liquid 204. After the first lower lock hopper valve 154 is closed, the first vacuum pump 146 is started immediately, the upper lock hopper 151 is vacuumized through the first air suction port 145, and after the preset vacuum degree is reached, the operation of pressurizing the upper lock hopper 151 through the first air charging valve 148 and the first air charging port 147 is repeated, so that the inert gas in the upper lock hopper 151 is balanced with the external pressure, and the feeding operation is realized. The feeding process of the balanced air pressure is the conventional operation of feeding solid materials into a vacuum, pressurizing chemical and metallurgical reactor.
The invention is not described in detail in the prior art, and therefore, the invention is not described in detail.
It will be understood that the terms "a" and "an" should be interpreted as referring to "at least one" or "one or more," i.e., in one embodiment, the number of elements may be one, while in another embodiment, the number of elements may be plural, and the term "a" should not be interpreted as limiting the number.
Although more use is made of the charging bin 101, the screw feeder 102, the first screw 103, the pyrolysis gas flue 104, the drying gas channel 105, the moisture evaporation hole 106, the flue gas baffle 107, the heat exchange fin 108, the drying gas collecting pipe 109, the pyrolysis gas temporary storage chamber 120, the pyrolysis oil condenser 121, the pyrolysis oil pressurizing pump 122, the pyrolysis mixed liquor condenser 123, the pyrolysis mixed liquor float tank 124, the pyrolysis floating oil pressurizing pump 125, the pyrolysis condensing water tank 126, the pyrolysis non-condensable gas booster pump 127, the pyrolysis non-condensable gas storage tank 128, the water treatment unit 130, the first suction inlet 145, the first vacuum pump 146, the first charging port 147, the first charging valve 148, the first high-pressure inert gas tank 149, the upper lock hopper 151, the lower lock hopper 152, the first upper lock hopper valve 153, the first lower lock hopper valve 154, the lead bismuth liquid circulation tank 201, the lead bismuth liquid standing tank 202, the lead bismuth liquid tank 203, the lead bismuth liquid 204, the stirring impeller 205, the heating chamber 206, the stirring shaft 206, the first suction port stirring motor 207, partition 208, feed port 209, hot air baffle 220, hot air inlet 221, hot air outlet 222, pyrolysis residue 301, pyrolysis residue spiral riser 302, second spiral 303, drain port 304, pyrolysis residue transition chamber 401, gasifier feed hopper 402, second upper lock hopper valve 403, second lower lock hopper valve 404, suction port 405, second vacuum pump 406, second fill port 407, second fill valve 408, second high pressure inert gas tank 409, dip feed upper pipe 501, dip feed lower pipe 502, molten bath gasifier 503, molten iron bath 504, oxygen lance 505, pyrolysis liquid nozzle 506, noncondensable gas injection pipe 507, syngas channel 508, one cold dust removal chamber 509, first lock hopper valve 510, one cold dust tank 511, two cold dust removal chamber 512, second lock hopper valve 513, two cold dust tank 514, final cold dust remover 515, third lock valve 516, final cold dust tank 517, syngas user 518, etc., but does not exclude the possibility of using other terms. These terms are used merely for convenience in describing and explaining the nature of the invention; they are to be interpreted as any additional limitation that is not inconsistent with the spirit of the present invention.
The present invention is not limited to the above-mentioned preferred embodiments, and any person can obtain various other products without departing from the scope of the present invention, but any changes in shape or structure are within the scope of the present invention, which is the same or similar to the present invention.
Claims (10)
1. Molten iron bath gasification furnace system with leading plumbum bismuth liquid whirl pyrolysis furnace, its characterized in that includes:
the lead-bismuth liquid circulation tank is internally provided with molten lead-bismuth liquid and a stirring mechanism for stirring the lead-bismuth liquid to form centrifugal rotational flow;
the feeding mechanism is used for sending the organic solid waste into the lead-bismuth liquid circulation tank for pyrolysis to generate pyrolysis gas;
the pyrolysis gas recovery mechanism is communicated with the pyrolysis gas outlet of the lead bismuth liquid circulation pool and is partially arranged outside the feeding mechanism, and is used for storing the pyrolysis gas to the pyrolysis gas temporary storage chamber and realizing the preheating of organic solid waste through the heat exchange between the pyrolysis gas and the outer wall of the feeding mechanism;
the pyrolysis gas condensation recovery mechanism is communicated with the pyrolysis gas temporary storage chamber and is used for converging and pressurizing part of pyrolysis liquid after first condensation in the pyrolysis gas temporary storage chamber and then spraying the part of pyrolysis liquid into the molten pool gasifier, and the rest part of pyrolysis gas is secondarily condensed and converged, and is kept stand for layering and respectively stored for recycling;
the lead bismuth liquid standing pool is communicated with the lead bismuth liquid circulation pool and is provided with a discharge mechanism for lifting and discharging pyrolysis residues floating on the surface of the lead bismuth liquid circulation pool;
a gasifier feed hopper for receiving pyrolysis residues discharged by the discharge mechanism and pressurizing and feeding the pyrolysis residues into the molten pool gasifier;
the molten pool gasifier is communicated with the gasifier feed hopper through an impregnation feeding upper pipe and an impregnation feeding lower pipe, and is internally provided with a molten iron bath pool filled with molten iron liquid, and is used for immersing the pyrolysis residues, the pyrolysis liquid and pyrolysis noncondensable gas into the molten iron bath pool to realize thorough pyrolysis-gasification, so as to obtain synthesis gas, and the synthesis gas is discharged through a synthesis gas channel;
the synthesis gas cooling treatment mechanism is communicated with the synthesis gas channel and is used for cooling the synthesis gas for a plurality of times, respectively storing the cooled synthesis gas, and finally filtering and dedusting the cooled synthesis gas to output clean normal-temperature synthesis gas;
and the heating chamber of the lead bismuth liquid pool is provided with a hot air inlet and a hot air outlet and is used for indirectly heating the lead bismuth liquid circulation pool and the lead bismuth liquid standing pool.
2. The molten iron bath gasifier system with a front lead-bismuth liquid cyclone pyrolysis furnace according to claim 1, wherein the pyrolysis gas recycling mechanism comprises a pyrolysis gas flue, a flue gas baffle and a drying gas channel, wherein the pyrolysis gas flue is arranged outside the feeding mechanism and is communicated with a pyrolysis gas outlet of the lead-bismuth liquid cyclone pool, the drying gas channel is used for prolonging a pyrolysis gas discharging path, increasing heat exchange time, and discharging drying gas, the top of the pyrolysis gas flue is communicated with the pyrolysis gas temporary storage chamber, and the pyrolysis gas recycling mechanism is further used for discharging the pyrolysis gas through the outer wall of the feeding mechanism for heat exchange, so that organic solid waste in the feeding mechanism is preheated.
3. The molten iron bath gasification furnace system with the lead-bismuth liquid cyclone pyrolysis furnace arranged in front of the furnace according to claim 2, wherein the feeding mechanism comprises a feeding bin, a spiral feeding pipe communicated with the feeding bin, a first spiral arranged in the spiral feeding pipe, a plurality of heat exchange fins arranged on the outer wall of the spiral feeding pipe and a drying gas collecting pipe for collecting the moisture evaporated by heating the escaped organic solid waste, the drying gas collecting pipe is communicated with the drying gas channel, and a plurality of moisture evaporation holes communicated with the drying gas collecting pipe are arranged on the spiral feeding pipe.
4. The molten iron bath gasifier system with the lead bismuth liquid cyclone pyrolysis furnace in front of claim 1, wherein the pyrolysis gas condensation recovery mechanism comprises a pyrolysis oil condenser for first condensing the pyrolysis gas discharged from the pyrolysis gas temporary storage chamber, a pyrolysis oil pressurizing pump for pressurizing the pyrolysis liquid, a pyrolysis liquid spray pipe for adding the pressurized pyrolysis liquid to the impregnation feeding down pipe, a pyrolysis mixed liquid condenser for secondarily condensing the pyrolysis gas, a pyrolysis noncondensable gas booster pump for pressurizing the remaining pyrolysis gas, and a pyrolysis noncondensable gas storage tank for storing the pressurized remaining pyrolysis gas, wherein the pyrolysis noncondensable gas storage tank adds the remaining pyrolysis gas to the molten bath gasifier through a noncondensable gas spray pipe.
5. The system of claim 4, wherein the pyrolysis mixed liquor condenser is further used for collecting a mixture of the pyrolysis liquor and water after secondary condensation, standing and layering, sending the pyrolysis liquor at the upper layer to the pyrolysis mixed liquor floating oil tank, pressurizing by the pyrolysis floating oil pressurizing pump, adding the pyrolysis liquor into the dipping feeding lower pipe by the pyrolysis oil spraying pipe, sending the water phase part at the lower layer to the pyrolysis condensation water tank, and processing the water phase part by the water treatment unit for recycling.
6. The molten iron bath gasification furnace system with the front lead-bismuth liquid cyclone pyrolysis furnace according to claim 1, wherein a partition wall is arranged on the lead-bismuth liquid standing pool, a plurality of liquid through holes are arranged on the partition wall to enable lead-bismuth liquid to pass through and block pyrolysis residues, the discharging mechanism comprises a pyrolysis residue spiral riser pipe which is obliquely arranged, a second spiral which is arranged in the pyrolysis residue spiral riser pipe, and a plurality of liquid leakage holes which are arranged on the pyrolysis residue spiral riser pipe, the pyrolysis residues are lifted and discharged through the second spiral, and lead-bismuth liquid entrained by the pyrolysis residues is recovered into the lead-bismuth liquid standing pool through the liquid leakage holes; the stirring mechanism comprises a stirring impeller arranged in the lead-bismuth liquid circulation tank and a stirring motor used for driving the stirring impeller, and the stirring motor is positioned outside the lead-bismuth liquid circulation tank and connected with the stirring impeller through a stirring shaft.
7. The molten iron bath gasifier system with lead bismuth liquid cyclone pyrolysis furnace in front of claim 1, wherein a plurality of hot air baffles are provided in the lead bismuth liquid bath heating chamber to extend hot air flow paths, increase heat exchange time and heat exchange area.
8. The molten iron bath gasification furnace system with the lead-bismuth liquid cyclone pyrolysis furnace arranged in front of claim 1, wherein a pyrolysis residue transition chamber is arranged at the top of the gasification furnace feed hopper, a second locking bucket valve is arranged between the pyrolysis residue transition chamber and the gasification furnace feed hopper, the gasification furnace feed hopper is further connected with a second vacuum pump and a second high-pressure inert gas tank, the second vacuum pump is used for vacuumizing the gasification furnace feed hopper through a second air suction port, the second high-pressure inert gas tank is used for filling inert gas into the gasification furnace feed hopper through a second air charging valve and an air charging port arranged on the gasification furnace feed hopper, and a second lower locking bucket valve is arranged between the bottom of the gasification furnace feed hopper and the upper dipping feeding pipe.
9. The molten iron bath gasification furnace system with the lead-bismuth liquid cyclone pyrolysis furnace arranged in front of the furnace according to claim 1, wherein the synthesis gas cooling treatment mechanism comprises a cold dust chamber, a second cold dust chamber and a final cold dust collector which are sequentially arranged along the advancing direction of the synthesis gas, a first lock bucket valve and a cold ash carrying tank are arranged at the bottom of the first cold dust chamber, a second lock bucket valve and a second cold ash carrying tank are arranged at the bottom of the second cold dust chamber, a third lock bucket valve and a final cold ash carrying tank are arranged at the bottom of the final cold dust collector, the final cold dust collector is used for discharging clean normal-temperature synthesis gas, and the first cold ash carrying tank, the second cold ash carrying tank and the second cold ash carrying tank are used for periodically collecting dust.
10. The molten iron bath gasification furnace system with the front lead-bismuth liquid cyclone pyrolysis furnace according to claim 1, wherein the feeding mechanism comprises an upper lock hopper provided with an upper lock hopper valve, a first vacuum pump for vacuumizing the upper lock hopper through a first air suction port, a first high-pressure inert gas tank for filling inert gas into the upper lock hopper through a first air charging valve and a first air charging port, a lower lock hopper arranged below the upper lock hopper and a first lock hopper valve arranged between the upper lock hopper and the lower lock hopper, a spiral pipe communicated with the center top of the lead-bismuth liquid circulating pool is arranged at the bottom of the lower lock hopper, a first spiral is arranged in the spiral feeding pipe, the bottom of the first spiral is connected with a stirring impeller of the stirring mechanism, and the stirring impeller is driven to rotate through the first spiral and simultaneously organic solid wastes are added into the lead-bismuth liquid circulating pool.
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| CN202210943784.6A CN117304984A (en) | 2022-08-08 | 2022-08-08 | Molten iron bath gasification furnace system with lead-bismuth liquid cyclone pyrolysis furnace arranged in front |
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| CN202210943784.6A CN117304984A (en) | 2022-08-08 | 2022-08-08 | Molten iron bath gasification furnace system with lead-bismuth liquid cyclone pyrolysis furnace arranged in front |
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| CN202210943784.6A Pending CN117304984A (en) | 2022-08-08 | 2022-08-08 | Molten iron bath gasification furnace system with lead-bismuth liquid cyclone pyrolysis furnace arranged in front |
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