CN117448019A - Pipeline type biomass pyrolysis hydrogen production equipment and method - Google Patents
Pipeline type biomass pyrolysis hydrogen production equipment and method Download PDFInfo
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- CN117448019A CN117448019A CN202310415920.9A CN202310415920A CN117448019A CN 117448019 A CN117448019 A CN 117448019A CN 202310415920 A CN202310415920 A CN 202310415920A CN 117448019 A CN117448019 A CN 117448019A
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 108
- 239000002028 Biomass Substances 0.000 title claims abstract description 62
- 239000001257 hydrogen Substances 0.000 title claims abstract description 59
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 59
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 54
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 28
- 238000000034 method Methods 0.000 title claims abstract description 28
- 238000007670 refining Methods 0.000 claims abstract description 61
- 238000007789 sealing Methods 0.000 claims abstract description 32
- 239000000463 material Substances 0.000 claims abstract description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 19
- 239000011229 interlayer Substances 0.000 claims abstract description 11
- 238000005338 heat storage Methods 0.000 claims abstract description 7
- 239000007789 gas Substances 0.000 claims description 30
- 230000008569 process Effects 0.000 claims description 12
- 238000003763 carbonization Methods 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 9
- 230000007246 mechanism Effects 0.000 claims description 9
- 239000001301 oxygen Substances 0.000 claims description 9
- 229910052760 oxygen Inorganic materials 0.000 claims description 9
- 238000010438 heat treatment Methods 0.000 claims description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 6
- 238000011049 filling Methods 0.000 claims description 5
- 150000002431 hydrogen Chemical class 0.000 claims description 5
- 239000010410 layer Substances 0.000 claims description 4
- 238000005096 rolling process Methods 0.000 claims description 4
- 238000001354 calcination Methods 0.000 claims description 3
- 239000000919 ceramic Substances 0.000 claims description 3
- 239000011819 refractory material Substances 0.000 claims description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 4
- 229910052799 carbon Inorganic materials 0.000 abstract description 4
- 239000000126 substance Substances 0.000 abstract description 3
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 16
- 239000003610 charcoal Substances 0.000 description 12
- 229910000831 Steel Inorganic materials 0.000 description 9
- 239000010959 steel Substances 0.000 description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 238000002360 preparation method Methods 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 229910002091 carbon monoxide Inorganic materials 0.000 description 4
- 229920000742 Cotton Polymers 0.000 description 3
- 239000000969 carrier Substances 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000009413 insulation Methods 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- 206010021143 Hypoxia Diseases 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 239000010425 asbestos Substances 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 229910052895 riebeckite Inorganic materials 0.000 description 2
- 239000003566 sealing material Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical class [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 230000013011 mating Effects 0.000 description 1
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000007306 turnover Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/05—Preparation or purification of carbon not covered by groups C01B32/15, C01B32/20, C01B32/25, C01B32/30
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses a pipeline type biomass pyrolysis hydrogen production device and a method, wherein the device comprises a pyrolysis refining furnace, an air outlet pipeline of the pyrolysis refining furnace is connected to a loop high-temperature furnace, a heat storage carrier is filled in the loop high-temperature furnace, and a superheated water vapor input pipe is arranged at the side edge of the loop high-temperature furnace; the pyrolysis refining furnace comprises a pipeline type pyrolysis furnace, and a pipeline type refining furnace is arranged below the pyrolysis furnace; a closed tank capable of translating along the pyrolysis furnace is arranged in the pyrolysis furnace, and two ends of the closed tank are respectively provided with a closed ring with a shape matched with the inner wall of the pyrolysis furnace, so that a sealing interlayer is formed between the closed tank and the pyrolysis furnace; a material frame which can translate in the closed tank is arranged in the closed tank; the sealed tank is provided with a one-way sealing valve, and the outer side of the pyrolysis furnace is provided with a telescopic connecting component for communicating the one-way sealing valve. The invention relates to equipment and a method for preparing hydrogen on the basis of preparing carbon by biomass pyrolysis, which can fully utilize substances and energy generated by biomass, and are more energy-saving and environment-friendly.
Description
Technical Field
The invention relates to hydrogen preparation equipment and a method, in particular to hydrogen preparation equipment and a method based on biomass pyrolysis.
Background
Hydrogen energy is a well-known clean energy source that is standing out as a low and zero carbon energy source. In the 21 st century, china and the United states, japan, canada, european Union and the like have made hydrogen energy development plans, and China has made various developments in the field of hydrogen energy, and is expected to become one of the countries with leading hydrogen energy technology and application in the near future, and is also internationally recognized as the country most likely to realize the industrialization of hydrogen fuel cells and hydrogen energy automobiles first.
Currently, the mainstream methods of industrial hydrogen production include: 1. the hydrogen production method by natural gas is to convert methane and water in natural gas into hydrogen and carbon dioxide at high temperature; 2. hydrogen is prepared by a method of electrolyzing water; electrolytic saturated saline (2nacl+2h2o= = energized= = 2naoh+h2 ++cl2 +). Obviously, no matter what method is adopted for preparing the hydrogen, certain requirements on energy sources, high temperature or electrifying are needed.
Biomass char production is an effective method for secondary utilization of biomass waste. In the process of preparing charcoal from biomass, pyrolysis of biomass under the action of different temperatures can produce wood gas composed of carbon monoxide and hydrogen, and methane and tar containing abundant polycyclic aromatic hydrocarbon can be released in the process of converting biomass into charcoal. The Chinese patent application 202211294894.0 discloses a multilayer tunnel type carbonization furnace, which adopts the technical scheme that biomass is transferred in tunnel type carbonization furnaces with different temperature ranges, so that the control of a biomass temperature curve is realized, and the charcoal can be manufactured more efficiently and simultaneously the useful gas generated in the charcoal manufacturing process can be recovered. The process of preparing the carbon can generate gas raw materials and energy required for preparing the hydrogen.
If the biomass charcoal making process and the industrial hydrogen making process can be organically integrated, the problems of energy and raw materials in hydrogen preparation can be effectively solved, and the energy utilization rate is higher, so that the method is more energy-saving and environment-friendly.
Disclosure of Invention
The invention aims to provide pipeline type biomass pyrolysis hydrogen production equipment and a pipeline type biomass pyrolysis hydrogen production method. The device and the method can complete hydrogen preparation on the basis of biomass pyrolysis charcoal preparation, can fully utilize substances and energy generated by biomass, and are more energy-saving and environment-friendly.
The technical scheme of the invention is as follows: the pipeline type biomass pyrolysis hydrogen production equipment is characterized by comprising a pyrolysis refining furnace, wherein an air outlet pipeline of the pyrolysis refining furnace is connected to a loop high-temperature furnace, a heat storage carrier is filled in the loop high-temperature furnace, and a superheated water vapor input pipe is arranged at the side edge of the loop high-temperature furnace; the pyrolysis refining furnace comprises a pipeline type pyrolysis furnace, and a pipeline type refining furnace is arranged below the pyrolysis furnace; both the pyrolysis furnace and the refining furnace are internally provided with a closed tank capable of translating along the pyrolysis furnace, two ends of the closed tank are respectively provided with a closed ring with a shape matched with the inner wall of the pyrolysis furnace, and the closed rings enable a sealing interlayer to be formed between the closed tank and the pyrolysis furnace; a material frame which can translate in the closed tank is arranged in the closed tank; the sealed tank is provided with a one-way sealing valve, and the outer side of the pyrolysis furnace is provided with a telescopic connecting component for communicating the one-way sealing valve. The pyrolysis refining furnace is used for carrying out pyrolysis and carbonization refining on biomass to finally generate a gas raw material for preparing hydrogen; the loop high temperature furnace is used for reacting the gas generated by the pyrolysis refining furnace with superheated steam and converting the gas into hydrogen.
In the pipeline type biomass pyrolysis hydrogen production equipment, the two ends of the pyrolysis furnace and the two ends of the refining furnace are respectively provided with a lifting transfer mechanism for lifting the closed tank.
In the pipeline type biomass pyrolysis hydrogen production equipment, the inner side of the closed tank is provided with the refractory material layer.
In the above-mentioned pipeline type biomass pyrolysis hydrogen production equipment, a coil is arranged in the refining furnace, and after the coil is connected with cold water, the coil can be heated by the temperature generated in the closed tank to form a water vapor raw material for generating superheated water vapor.
In the pipeline type biomass pyrolysis hydrogen production equipment, the refining furnace body is divided into a plurality of sections, and a driving wheel for rolling the refining furnace body is arranged on the outer side of one section. The section is arranged to turn over the material in the final step of converting biomass into charcoal so that the heated material is more uniform and the properties of the produced charcoal in the same batch are similar.
In the pipeline type biomass pyrolysis hydrogen production equipment, the loop high-temperature furnace comprises a main furnace body, and a plurality of baffling retaining walls are arranged on the inner side of the main furnace body; the front end of the main furnace body is provided with an air inlet, the rear end is provided with an air outlet, and the side edge is provided with a superheated steam input pipe. The baffle retaining wall forms a long-stroke return structure in the furnace, and the reaction area is increased.
In the pipeline type biomass pyrolysis hydrogen production equipment, the heat storage carriers are ceramic balls, so that the heat storage and heat preservation can be performed on the whole reaction zone, and the contact probability between gases can be increased due to the porous structure formed between the heat storage carriers.
The method for preparing hydrogen by the pyrolysis of the pipeline type biomass is characterized by comprising the following steps of:
(1) filling biomass blanks on a material frame of a closed tank, and sealing the closed tank;
(2) moving the closed tank along the pyrolysis furnace, staying for set time in different sections of the pyrolysis furnace, and inputting heat into an interlayer between the closed tank and the pyrolysis furnace in the stay time period of the closed tank to heat the closed tank; by setting the heat input values of different sections of the pyrolysis furnace, the temperature in the tube gradually rises from the room temperature when the closed tank passes through the different sections, and biomass blanks in the closed tank are subjected to dry distillation under an anaerobic environment;
(3) feeding the gas generated by carbonization into a loop high-temperature furnace to react with superheated steam to generate mixed gas containing hydrogen, and separating the hydrogen from the mixed gas;
(4) the closed tank enters a refining furnace through a lifting transfer mechanism and moves along the refining furnace, the different sections of the refining furnace stay for set time, superheated steam is input into the closed tank, the temperature in the closed tank is increased to the calcining temperature, the biomass blank is further carbonized, and the gas generated in the closed tank and the other gases obtained in the step (2) are dry distilled and enter a return high-temperature furnace;
(5) continuously moving the closed tank forwards, and introducing oxygen into the closed tank to enable carbonized biomass blanks on the material frame to be partially oxidized in a low-oxygen state, so that the closed tank reaches the high temperature required by refining;
(6) the heat generated in the closed tank (31) heats water in a coil pipe in the refining furnace (4) to generate steam, the steam is secondarily heated to be converted into superheated steam, the superheated steam is sent into a return high-temperature furnace, and the hot gas generated in the closed tank (31) is sent into the pyrolysis furnace to be used as a heat source.
In the above-mentioned method for producing hydrogen by pipe-type biomass pyrolysis, in the step (6), the refining furnace is divided into a plurality of sections, wherein one section is integrally turned over in the refining process, so that the material in the closed tank is prevented from being heated unevenly.
In the method for preparing hydrogen by pipe-type biomass pyrolysis, after the step (6), fire extinguishing and cooling are carried out in the closed tank, then discharging is carried out, and filling is restarted to enter the next working procedure.
Compared with the prior art, the biomass pyrolysis charcoal making technology and the natural gas hydrogen making technology are combined, the co-production of charcoal making and hydrogen making can be realized, and substances and energy generated in the biomass pyrolysis charcoal making process can be effectively applied in the hydrogen making process, so that the biomass pyrolysis charcoal making technology has the advantages of less waste discharge, low energy consumption and the like.
On the basis of the technical scheme of the multilayer tunnel type carbonization furnace in the Chinese patent application 202211294894.0, the tunnel kiln is changed into a pipeline type furnace body, the closed tank is additionally arranged in the furnace body, and the closed tank is sealed and can form a sealing interlayer with the inner wall of the furnace body, so that the sealing performance of the material is better when the material is pyrolyzed (dry distilled) in the closed tank. Meanwhile, the closed interlayer is arranged so that the closed tank is equivalent to a kiln chamber (the movement replaces the temperature adjustment) which enters different temperature control intervals when moving to different sections in the pipeline type furnace body, and the temperature does not need to be continuously adjusted like the existing carbonization chamber.
The invention also provides a method for refining materials in the oxygen-feeding refining furnace body under the condition of oxygen deficiency and oxygen deficiency by inputting oxygen into the closed tank and controlling the oxygen-feeding amount, wherein partial oxidation reaction can occur in the process to generate a large amount of heat energy, so that on one hand, the refining temperature can be further improved, the quality of the finished carbon such as density and conductivity can be improved, and on the other hand, the redundant heat can be used for heat supply of biomass pyrolysis and heat supply during superheated steam preparation, thereby reducing external energy supply.
Drawings
FIG. 1 is a schematic view of the external structure of a loop high temperature furnace of the present invention;
FIG. 2 is a schematic view of the structure of the loop high temperature furnace of the present invention;
FIG. 3 is a schematic view of the structure of the closed tank of the present invention;
fig. 4 is an enlarged view of a portion a of fig. 3;
FIG. 5 is a schematic view of the mating structure of the one-way sealing valve and the telescopic connection assembly in an embodiment of the present invention;
FIG. 6 is a schematic diagram of a pyrolysis furnace in accordance with an embodiment of the present invention;
FIG. 7 is a schematic cross-sectional structure of a pyrolysis furnace according to an embodiment of the present invention;
FIG. 8 is a schematic view of a rolling structure of a refining furnace according to an embodiment of the present invention.
Detailed Description
The invention is further illustrated by the following figures and examples, which are not intended to be limiting.
Examples: the pipeline type biomass pyrolysis hydrogen production equipment mainly comprises a loop high-temperature furnace and a pyrolysis refining furnace:
the structure of the loop high-temperature furnace is shown in fig. 1 and 2, and comprises a main furnace body 22, wherein a plurality of baffling retaining walls 23 are arranged on the inner side of the main furnace body 22; the main furnace body 22 is provided with an air inlet at the front end, an air outlet at the rear end and a superheated steam input pipe 21 at the side. The main furnace body 22 is composed of an outer frame made of I-steel, and is surrounded by an inner welding steel plate which surrounds the inner refractory castable. The middle part of the main furnace body 22 can be provided with a heat insulating device to divide the main furnace body into two parts, and the two parts are respectively provided with an air inlet and an air outlet. The heat accumulating carrier is filled in the loop high-temperature furnace, and the heat accumulating carrier is ceramic balls which can also be used as catalyst carriers.
The pyrolysis furnace has a core structure of a closed tank 31, as shown in fig. 3 and 4, two ends of the closed tank 31 are respectively provided with a closed ring 32 with a shape matched with the inner wall of the pyrolysis furnace 3, and the closed rings 32 form a sealing interlayer between the closed tank 31 and the pyrolysis furnace 3; the closed ring 32 may be made of an annular I-steel 321, and the I-cylinder may be welded to the closed tank 31 to form a cavity inside and a caulking groove outside, and asbestos 322 may be disposed in the caulking groove as a sealing material. The airtight can 31 is closed at one end and opened at the other end, and is provided with an airtight door 311 opened laterally. The pyrolysis furnace 3 is provided with a smoke exhaust valve. To increase the life of the closed vessel, the closed vessel may be constructed from steel tubing, structural nails welded to the inside of the steel tubing, and then a layer of refractory material 312 is poured.
A material frame 33 which can translate in the closed tank 31 is arranged in the closed tank 31; the closed tank 31 is provided with a one-way closed valve 34, and the outer side of the pyrolysis furnace 3 is provided with a telescopic connecting component 35 for communicating the one-way closed valve 34. Rollers 36 are provided on the outside of the closed vessel 31 and the material frame 33 for movement along the furnace and vessel, respectively. The outer sides of the closed tank 31 and the material frame 33 can be provided with a positioning guide mechanism 37 (similar to the matching structure of the elevator guide rail and the guide shoe) so that the closed tank is not easy to incline and turn.
As shown in fig. 5, the matching relationship between the unidirectional sealing valve 34 and the telescopic connecting assembly 35 is that the unidirectional sealing valve 34 comprises a hollow valve body 341, a step is arranged in the valve body 341, a circle of sealing ring 342 is arranged on the step, a valve core 343 is also arranged in the valve body 341, and the valve core 343 is pressed against the sealing ring 342 from the inner side to the outer side of the sealing tank 31 through a spring 344; the telescopic connection assembly 35 comprises a jacking pipe 351 with a front end, wherein a plurality of protrusions 352 are arranged at the front end of the jacking pipe, a circle of sealing interface 353 with the shape being attached to the outer side of the closed tank 31 is arranged at the middle section of the jacking pipe 351, asbestos can be arranged on the sealing interface 353 to serve as a sealing material, the rear end of the jacking pipe 351 is arranged on a telescopic cylinder, and the tail of the jacking pipe 351 is connected with other gas pipelines to be connected through telescopic pipes such as corrugated pipes.
When the unidirectional sealing valve 34 and the telescopic connecting assembly 35 are needed, only the jacking pipe 351 is needed to jack in the direction of the unidirectional sealing valve 34, when the jacking pipe 351 jacks the valve core 343, the sealing interface 353 is tightly adhered to the sealing tank 31, and the inside of the sealing tank 31 is communicated with the jacking pipe and is not communicated to the sealing interlayer. When the push pipe 351 is withdrawn, the valve core 343 is restored under the action of the spring 344.
The pyrolysis furnace structure principle is as shown in fig. 6 and 7, and mainly comprises a pyrolysis furnace 3 and a lower refining furnace 4:
the pyrolysis furnace 3 and the refining furnace 4 are long steel pipes, heat insulation cotton is arranged on the outer side of the steel pipes, the length of the heat insulation cotton can be set according to the length of the closed tank 31, a plurality of closed tanks 31, for example 9 heat insulation cotton can be arranged and contained in the closed tank, the pyrolysis furnace 3 can be divided into 9 sections, fixed heat energy can be introduced into each section, the closed tank 31 can be made to be different in temperature when moving to different sections, a setting mode that the temperature is gradually increased along the moving direction of the closed tank 31 can be adopted, and specific temperature values can be selected by using a temperature curve required by the type pyrolysis of biomass materials. The temperature in the pyrolysis furnace 3 can be heated by inputting hot gas generated by the lower-end refining furnace 4 into the sealing interlayer, arranging heating wire heat conduction oil, or directly inputting superheated steam into the closed tank 31, or can be used by adopting a plurality of heat sources in a matching way. If it is necessary to reduce the dependence on external energy, a certain amount of oxygen may be supplied into the closed tank 31 to oxidize a part of biomass and generate heat.
The rear end of the refining furnace 4 can be provided with a cooling furnace, the cooling furnace has lower requirement, and the material frame can be closed after being fed, and can be subjected to fire extinguishing and cooling by filling carbon dioxide and the like.
The refining furnace body 4 is provided with a rotatable section, and a driving wheel 42 for rolling the refining furnace body 4 is arranged outside the rotatable section. As shown in fig. 8.
The movement of the closed tanks 31 can push the closed tanks 31 into the furnace in sequence through the hydraulic ejector rods outside the furnace, and the rear closed tank 31 pushes the front closed tank 31 to move, so that the problem that the overall sealing effect in the furnace is reduced due to the fact that a power mechanism is arranged inside the furnace can be avoided. Of course, the device can also be realized by means of a reciprocating channel steel traction mechanism arranged in the pyrolysis furnace 3 and the refining furnace 4, and the reciprocating channel steel traction mechanism can adopt the same structure in a multilayer tunnel type carbonization furnace of China patent application 202211294894.0.
The device of the invention carries out carbonization in the closed tank, can adopt the external isolation high-temperature heating and the selective waste gas circulation heating of the lower-layer refining furnace 4, has high energy utilization rate and lower cost, and the mixed gas of methane and carbon monoxide discharged by the pyrolysis in the sealed tank is conveyed to the return high-temperature furnace through the sealing pipe interface for use as raw materials, thus the utilization rate of intermediate products is higher.
The invention relates to a pipeline type biomass pyrolysis hydrogen production method, which comprises the following steps:
(1) filling biomass blanks on a material frame of a closed tank, and sealing the closed tank;
(2) moving the closed tank along the pyrolysis furnace, staying for set time in different sections of the pyrolysis furnace, and inputting heat into an interlayer between the closed tank and the pyrolysis furnace in the stay time period of the closed tank to heat the closed tank; by setting the heat input values of different sections of the pyrolysis furnace, the temperature in the tube gradually rises from the room temperature when the closed tank passes through the different sections, and biomass blanks in the closed tank are subjected to dry distillation under an anaerobic environment; the pyrolysis furnace temperature can be set to preheat from room temperature and then to about 300 ℃ finally, because biomass can undergo a large amount of pyrolysis reaction in the temperature range to generate methane, carbon monoxide and other gases.
(3) The gas (solid particles and tar to be filtered) generated by carbonization is sent into a loop high-temperature furnace to react with superheated steam to generate mixed gas containing hydrogen, and the hydrogen is separated from the mixed gas; the temperature in the loop high-temperature furnace is controlled between 800 and 1200 ℃. The process is primarily to react methane and carbon monoxide with steam to produce hydrogen and carbon dioxide. And (3) after the mixed gas is subjected to heat exchange and cooling, separating out hydrogen by utilizing a compression separation technology.
(4) The closed tank enters a refining furnace through a lifting transfer mechanism, firstly, superheated steam is input into the closed tank, the temperature in the closed tank is increased to a calcining temperature, biomass blanks are further carbonized, and gas generated in the closed tank and other gases obtained in the step (2) through dry distillation enter a return high-temperature furnace; the temperature in the refining furnace can be gradually heated to about 600 ℃ along the advancing direction.
(5) Continuously moving the closed tank forwards, and introducing oxygen inwards to enable carbonized biomass blank to be partially oxidized in a low-oxygen state, so that the carbonized biomass blank enters the closed tank to reach the high temperature required by refining; the refining temperature can be gradually heated to about 1200 ℃ along the advancing direction.
(6) The water in the coil 41 in the refining furnace 4 in the step (5) can be heated by the heat generated by the closed tank to generate water vapor, the water vapor is heated for the second time to be converted into superheated water vapor, the superheated water vapor is sent into the loop high-temperature furnace, and the hot gas generated by the oxygen-feeding refining furnace body is sent into the pyrolysis furnace to be used as a heat source. The water vapor generated by heating the oxygen-feeding refining furnace body is generally low in temperature, the temperature can be continuously raised through heat exchange in the step (3), and the water vapor can be heated to the superheated water vapor with the required temperature through an electromagnetic heating mode.
In the step (6), the refining furnace body is divided into a plurality of sections, and the last section is integrally turned over in the refining process, so that uneven heating of material flows in the furnace is avoided;
after step (6), fire extinguishing and cooling are needed in the closed tank 31, a section of cooling furnace can be arranged, oxygen input into the closed tank is stopped or nitrogen/carbon dioxide is directly input into the closed tank for fire extinguishing, and then cold water is input into the coil pipe for heat exchange and cooling.
Claims (10)
1. A pipeline type biomass pyrolysis hydrogen production device is characterized in that: the device comprises a pyrolysis refining furnace, wherein an air outlet pipeline of the pyrolysis refining furnace is connected to a return high-temperature furnace, a heat storage carrier is filled in the return high-temperature furnace, and a superheated water steam input pipe (21) is arranged at the side edge of the return high-temperature furnace; the pyrolysis refining furnace comprises a pipeline type pyrolysis furnace (3), and a pipeline type refining furnace (4) is arranged below the pyrolysis furnace (3); both the pyrolysis furnace (3) and the refining furnace (4) are internally provided with a closed tank (31) which can translate along the pyrolysis furnace (3), two ends of the closed tank (31) are respectively provided with a closed ring (32) with the shape matched with the inner wall of the pyrolysis furnace (3), and the closed rings (32) form a sealing interlayer between the closed tank (31) and the pyrolysis furnace (3); a material frame (33) which can translate in the closed tank (31) is arranged in the closed tank (31); the sealed tank (31) is provided with a one-way sealing valve (34), and the outer side of the pyrolysis furnace (3) is provided with a telescopic connecting component (35) for communicating the one-way sealing valve (34).
2. The pipeline biomass pyrolysis hydrogen production apparatus of claim 1, wherein: and lifting and transferring mechanisms for lifting the closed tank (31) are arranged at two ends of the pyrolysis furnace (3) and the refining furnace (4).
3. The pipeline-type biomass pyrolysis hydrogen production apparatus according to claim 2, characterized in that: a refractory material layer (312) is arranged on the inner side of the closed tank (31).
4. A pipeline biomass pyrolysis hydrogen plant according to claim 3 wherein: a coil pipe (41) is arranged in the refining furnace (4).
5. A pipeline biomass pyrolysis hydrogen plant according to claim 3 wherein: the refining furnace (4) is divided into a plurality of sections, wherein a driving wheel (42) for rolling the refining furnace (4) is arranged on the outer side of one section.
6. The pipeline biomass pyrolysis hydrogen production apparatus of claim 1, wherein: the return high-temperature furnace comprises a main furnace body (22), and a plurality of baffling retaining walls (23) are arranged on the inner side of the main furnace body (22); the front end of the main furnace body (22) is provided with an air inlet, the rear end is provided with an air outlet, and the side edge is provided with a superheated steam input pipe (21).
7. The pipeline biomass pyrolysis hydrogen production apparatus of claim 1, wherein: the heat storage carrier is a ceramic ball.
8. A pipeline biomass pyrolysis hydrogen production process based on any one of claims 1 to 7, comprising the steps of:
(1) filling biomass billets on a material frame (33) of a closed tank (31), and sealing the closed tank (31);
(2) moving the closed tank (31) along the pyrolysis furnace (3), staying at different sections of the pyrolysis furnace (3) for a set time, and inputting heat into an interlayer between the closed tank (31) and the pyrolysis furnace (3) in the stay time of the closed tank (31) to heat the closed tank (31); by setting the heat input values of different sections of the pyrolysis furnace (3), the temperature in the tube gradually rises from the room temperature when the closed tank (31) passes through the different sections, and biomass blanks in the closed tank (31) are subjected to dry distillation under an anaerobic environment;
(3) feeding the gas generated by carbonization into a loop high-temperature furnace to react with superheated steam to generate mixed gas containing hydrogen, and separating the hydrogen from the mixed gas;
(4) the closed tank (31) enters the refining furnace (4) through the lifting transfer mechanism, moves along the refining furnace (4), stays for set time in different sections of the refining furnace (4), inputs superheated steam into the closed tank (31), increases the temperature in the closed tank (31) to the calcining temperature, further carbonizes the biomass blank, and the gas generated in the closed tank (31) and the gas generated in the step (2) enter the return high-temperature furnace (2) together after being subjected to dry distillation;
(5) continuously moving the closed tank (31) forwards, and introducing oxygen into the closed tank (31) to enable carbonized biomass blank on the material frame (33) to be partially oxidized in a low-oxygen state, so that the interior of the closed tank (31) reaches the high temperature required by refining;
(6) the heat generated in the closed tank (31) heats water in a coil pipe (41) in the refining furnace (4) to generate steam, the steam is secondarily heated to be converted into superheated steam, the superheated steam is sent into a high-temperature return furnace, and hot gas generated in the closed tank (31) is sent into the pyrolysis furnace (3) to be used as a heat source.
9. The method for producing hydrogen by pipe-type biomass pyrolysis according to claim 8, wherein: in the step (6), the refining furnace (4) is divided into a plurality of sections, wherein one section is integrally turned over in the refining process, and the uneven heating of materials in the closed tank (31) is avoided.
10. The method for producing hydrogen by pipe-type biomass pyrolysis according to claim 8, wherein: and (3) after the step (6), extinguishing fire and cooling the sealed tank (31).
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| CN202310415920.9A CN117448019A (en) | 2023-04-14 | 2023-04-14 | Pipeline type biomass pyrolysis hydrogen production equipment and method |
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