CN105861072A - Method and system for preparing high-concentration CO from waste carbon - Google Patents
Method and system for preparing high-concentration CO from waste carbon Download PDFInfo
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- CN105861072A CN105861072A CN201610406051.3A CN201610406051A CN105861072A CN 105861072 A CN105861072 A CN 105861072A CN 201610406051 A CN201610406051 A CN 201610406051A CN 105861072 A CN105861072 A CN 105861072A
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- 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
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- 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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- 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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0903—Feed preparation
- C10J2300/0906—Physical processes, e.g. shredding, comminuting, chopping, sorting
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- 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
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
- C10J2300/1612—CO2-separation and sequestration, i.e. long time storage
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- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The invention belongs to the technical field of solid waste resourceful treatment, and relates to a method and system for preparing high-concentration CO from waste carbon. The method includes the steps that waste is pretreated, and a waste raw material is pyrolyzed in a revolving bed pyrolyzing furnace to obtain pyrolytic carbon and pyrolytic oil gas; a crusher crushes the pyrolytic carbon, the pyrolytic oil gas is treated through an energy-saving deacidifying device and an oil gas separating and purifying device to obtain pyrolysis gas, and CO2 gas is separated from the pyrolysis gas through a CO2 capturing device; the crushed pyrolytic carbon and the separated CO2 gas enter a fluidized bed gasifier to be gasified so as to generate gasified gas CO. The waste carbon is used as the gasification raw material, high-concentration CO2 is captured from pyrolysis gas to serve as a gasifying agent to prepare the high-concentration CO, the method is applied to the direct reduction ironmaking technology of a gas-based shaft kiln, and the whole technology is low in carbon emission and good in environmental protection benefits.
Description
Technical field
The invention belongs to the technical field that solid waste resource recovery processes, relating to one with rubbish charcoal is
The method and system of high concentration CO prepared by raw material.
Background technology
China is faced with the dual-pressure of environment and the energy, the acceleration being in progress along with economy and urbanization,
Whole nation energy resource consumption is huge, and most big cities face garbage-surrounded city predicament, will by technological means
House refuse becomes available resources, can alleviate China's energy and environmental crisis to a certain extent.
Domestic garbage pyrolysis technology is high with its resource utilization rate, and the little advantage of environmental pollution is increasingly by people
Favored.Domestic garbage pyrolysis primary product has following several: partial thermal decomposition oil can conduct by refining
Fuel oil uses；Some low-molecular-weight hydrocarbons such as hydrogen can be included as the pyrolysis gas that fuel gas uses
Gas, methane, carbon monoxide etc.；Rubbish charcoal major part exists with white carbon black form, but there is heavy metal etc.
Poisonous and harmful substance, calorific value is low, and market outlet is poor；If used as solid fuel, burning effect
The most poor, and combustion process can produce a large amount of secondary pollution, environmental benefit is poor.Therefore, greatly
Most rubbish charcoals finally carry out landfill disposal only as pyrolysis residue, land occupation resource and cause energy
The waste in source.
The pyrolysis gas that house refuse produces after pyrolysis contains the CO of about 30%2, CO2Existence can drop
Low pyrolysis gas calorific value, reduces its utilization ways, and economic benefit is poor.Pyrolytic carbon major part is with white carbon black shape
Formula exists, and is good gasified raw material, if using the CO in pyrolysis gas2It is oxidized as gasifying agent
Become CO, on the one hand can be substantially reduced because burning the problem of environmental pollution that pyrolytic carbon is brought, on the other hand,
Reduce CO in pyrolysis gas2Content, improves CO content, improves pyrolysis gas calorific value.
The open one way of life refuse pyrolysis resource of patent documentation (patent No. 201420457702.8) is combined
Close processing system, this system by house refuse after the pretreatment such as sorting, broken, drying, molding,
In pyrolysis oven, it is pyrolyzed to obtain high-temperature oil gas and rubbish charcoal, after the gasification of rubbish charcoal, generates gasification combustible gas,
In order to the fuel as heat storage type gas radiation pipe burner.
Owing to this system uses the air frowzy and the flue gas of moisture vapor produced in preprocessing process
As the gasifying agent of rubbish charcoal, the combustible gas calorific value that gasification produces is low, and value is low, gasifies simultaneously
Gas directly burns, and does not collect CO in flue gas2, charcoal discharge capacity is big, and environmental benefit is poor.This system uses
Rubbish charcoal is gasified by gasification technology, it is achieved rubbish charcoal resource, but in product reducibility gas concentration is relatively
Low, it is impossible to directly apply to shaft furnace iron-smelting process.
The announcement one adverse current reincarnation rubbish alive of another patent documentation (patent No. 201210143133.5)
Rubbish pyrolytic carbon gasification furnace system and garbage treating process, this system mainly includes feed arrangement, rubbish carbonization
Furnace body, spiral organ of Corti of slagging tap, pyrolysis gas incinerator, circulating fan, air preheater, aerator,
The equipment such as pipeline valve, and combine the air and heat circulating device that is connected with rubbish carbonization furnace body and carried out
Kind, coordinate rubbish carbonization furnace body temperature, the control of the rubbish time of staying, it is achieved to house refuse
And organic solid castoff processes, the product pyrolysis gas that this patent obtains is directly entered incinerator combustion
Burning the high-temperature flue gas producing 850 DEG C-1100 DEG C, rubbish charcoal is as final products.
Foregoing invention is, under conditions of heating anaerobic, house refuse and organic solid waste are resolved into combustible gas
Body and breeze, combustible gas directly burns, and is not carried out CO2Recycle, there is charcoal discharge capacity big, ring
The shortcoming that border is of poor benefits.Additionally, foregoing invention is as final products using rubbish charcoal, due to rubbish charcoal
Calorific value is relatively low, and market outlet is not smooth, and containing poisonous and harmful substances such as heavy metals, if by rubbish charcoal
The most poor as final products, economic benefit and environmental benefit, Technique Popularizing is relatively difficult.
In sum, prior art is not by the CO in domestic garbage pyrolysis gas2As gasifying agent, rubbish
Rubbish charcoal produces high concentration CO as gasified raw material, and is applied to gas-based shaft kiln directly reduced ironmaking work
Skill, while realizing rubbish charcoal resource, not only improves pyrolysis gas calorific value but also meets CO2Recycle.
Summary of the invention
For the problems referred to above, the main object of the present invention is to provide prepares high concentration with rubbish charcoal for raw material
The method and system of CO, by the CO in domestic garbage pyrolysis gas2As gasifying agent, rubbish charcoal is as gasification
Raw material production high concentration CO, and applied at gas-based shaft kiln directly reduced iron-smelting process.
The present invention provides a kind of method preparing high concentration CO for raw material with rubbish charcoal, and it includes following
Step:
Pretreatment: rubbish sequentially passes through broken bag, roller screen, sorting and break process, obtains garbage raw material；
Refuse pyrolysis: send into the described garbage raw material of revolving bed pyrolysis oven through being dried, be pyrolyzed and activating
Reaction, the material obtained includes pyrolytic carbon, pyrolysis oil gas；
Broken pyrolytic carbon: through the described pyrolytic carbon particle diameter ＜ 10mm of crusher in crushing；
Energy-conservation deacidification and isolation of purified: described pyrolysis oil gas is clean through energy-conservation deacidifying device and Oil-gas Separation
Gasifying device processes, and obtains pyrolysis gas；
CO2Trapping: described pyrolysis gas is through CO2Capturing device processes, and isolates CO2Gas；
Fluidized-bed gasification furnace gasify: described in isolate CO2Described stream is entered with the described pyrolytic carbon after broken
Changing bed gasification furnace to gasify, the gasification temperature of fluidized-bed gasification furnace is 900-1100 DEG C, produces gasification
Gas CO.
At described CO2In trapping step, described pyrolysis gas enters CO2The absorption tower of capturing device, is inhaling
Contact with alkanolamine solution in receiving tower, the CO in described pyrolysis gas2Absorbed by described alkanolamine solution and become rich
Liquid, described rich solution is pumped into desorber through rich solution, mixed gas after desorbing and and lean solution cooled
Device cooling down, the mixed gas after cooling enters gas-liquid separator, isolates CO2Gas.
In fluidized-bed gasification furnace gasification step, the gas CO that gasifies described in a part for generation erects as gas base
The reducing agent of stove reduction iron production, the CO of generation2Gas sends into described fluidized-bed gasification furnace；Another part institute
State gasification gas CO and send into described revolving bed pyrolysis oven.
After the described pyrolysis oil gas obtained after the refuse pyrolysis process by described energy-conservation deacidification, described heat
The temperature solving oil gas is down to 250 DEG C-350 DEG C, sour gas volumetric concentration 0.05%；Described oil gas divides
Wet dedusting tower in purifier uses 70-80 DEG C of Quench recirculated water to spray described pyrolysis oil gas, real
Existing dedusting and pyrolysis oil, the separation of pyrolysis gas, the described pyrolysis gas after dedusting cools down in primary cooler,
It is then fed into detar in electrical tar precipitator, then by aerator, pyrolysis gas is delivered to desulfurizing tower and denitrating tower,
Produce pure pyrolysis gas；Described primary cooler recirculated water and chilled water are by described pyrolysis oil air cooling extremely
20-25 DEG C, the temperature of described recirculated water and described chilled water is respectively 30-35 DEG C and 15-20 DEG C.
The particle diameter ＜ 20mm of the pretreated described garbage raw material of rubbish, the moisture content of described garbage raw material
For 20%-60%.In described revolving bed pyrolysis oven, described garbage raw material layer thickness is 50-250mm.
The present invention also provides for a kind of realization
System, comprising:
Rubbish pretreatment unit: by broken bag mechanism, roller screen mechanism, sorting mechanism and crushing mechanism successively
Connecting and composing, described mechanism is respectively provided with charging aperture and discharging opening；
Revolving bed pyrolysis oven: by dry section, pyrolytic reaction one district, pyrolytic reaction two district and pyrolytic reaction
3rd district are constituted, and the top in each described district has pyrolysis oil gas vent, the radial canal in each described district to have combustion
Gas air inlet；There are garbage raw material entrance, the end in described pyrolytic reaction three district in the front end of described dry section
There is pyrolytic carbon discharging opening；
The charging aperture of disintegrating machine is connected with described pyrolytic carbon discharging opening, the storage charcoal groove outlet of described disintegrating machine
It is connected with the pyrolytic carbon charging aperture of fluidized-bed gasification furnace；
Described revolving bed pyrolysis oven, energy-saving denitration device, Oil-gas Separation purifier, CO2Capturing device
It is sequentially connected with described fluidized-bed gasification furnace.
Further, the pyrolysis oil gas air inlet of described energy-saving denitration device and described revolving bed pyrolysis oven
Pyrolysis oil gas vent be connected；
Described Oil-gas Separation purifier is by oil pyrolysis gas pipeline, wet dedusting tower, primary cooler, electric fishing
Tar device, aerator, desulfurizing tower, denitrating tower are sequentially connected with composition；Described oil pyrolysis gas pipeline and institute
The pyrolysis oil gas vent stating energy-saving denitration device is connected.
Described CO2Capturing device by absorption tower, rich solution pump, desorber, reboiler, gas-liquid separator,
Lean pump and lean solution cooler are sequentially connected with composition；The air inlet on described absorption tower and described energy-saving denitration
The gas outlet of the denitrating tower of device is connected, the gas outlet of described gas-liquid separator and described fluidized gasification
The air intake of stove is connected.
At described CO2Absorption tower in capturing device, bottom the entrance of described rich solution pump and described absorption tower
Second outlet is connected；Desorber the first entrance phase on described rich solution delivery side of pump and described desorber top
Even；The entrance of described lean pump is connected with desorber the first outlet bottom described desorber；Described again
The entrance of boiling device is connected with desorber the second outlet bottom described desorber, and described desorber second enters
Mouth is connected with the outlet of described reboiler, gas described in desorber the 3rd outlet at described desorber top
Liquid/gas separator entrance, the outlet of described lean pump is connected with the entrance of described lean solution cooler.
The air inlet of air accumulator exports with the gasification gas of described fluidized-bed gasification furnace and is connected, described air accumulator
The first gas outlet be connected with the gas inlet of described revolving bed pyrolysis oven, the second of described air accumulator
Gas outlet is connected with gas-based shaft kiln.
The pyrolysis gas that house refuse produces after pyrolysis contains the CO of about 30%2, due to CO2It is can not
Combustion gas body, its existence can reduce the calorific value of pyrolysis gas, and the economic benefit of generation is poor.The big portion of rubbish charcoal
Divide and exist with white carbon black form, be good gasified raw material.Use the method and system of the present invention, pass through
CO2Trapping technique is by the CO in pyrolysis gas2Separation and collection, then prepares as gasifying agent gasification rubbish charcoal
High concentration CO gas, a part of CO can be as the reducing agent of gas-based shaft kiln directly reduced ironmaking, by-product
Product high concentration CO2, may return to fluidized-bed gasification furnace as gasifying agent.A part of CO can do and rotate
Bed radial canal supplements fuel.One aspect of the present invention can solve the environmental pollution brought because of charcoal of burning away the refuse
Problem, on the other hand, CO in separation and collection pyrolysis gas2, improve the calorific value of pyrolysis gas, it is achieved rubbish charcoal
Resource, also can realize CO simultaneously2Internal process recycles, and reduces charcoal discharge capacity, is conducive to improving
Whole domestic garbage pyrolysis processes economic benefit and the environmental benefit of technique.
The beneficial effects of the present invention is:
Employing revolving bed pyrolysis oven is as domestic garbage pyrolysis oil gas and the equipment of pyrolysis oil gas charcoal, same
Completing the process being dried, being pyrolyzed in one stove, flow process is short, and energy utilization rate is high, is easily achieved simultaneously
Scale.
From revolving bed pyrolysis oven pyrolysis oil gas out through energy-conservation deacidifying device, realize waste heat simultaneously and return
Receive and the removing of sour gas, improve energy utilization efficiency, alleviate the sour gas corrosion to equipment.
With rubbish charcoal as gasified raw material, the high concentration CO of trapping from pyrolysis gas2As gasifying agent vaporizing system
Standby high concentration CO, and it is applied to gas-based shaft kiln directly reduced iron-smelting process, whole technique, carbon is arranged
The lowest, environmental benefit is strong；Also solve rubbish charcoal calorific value low simultaneously, the problem that market outlet is the most smooth,
High financial profit.
Use the present invention, CO2The response rate reaches more than 90%, and purity reaches more than 98%.High-purity CO2With rubbish
Rubbish charcoal carries out gasification reaction at normal pressure, at 1200 DEG C, and charcoal conversion ratio reaches more than 97%.CO in gasification gas
Purity reaches more than 98%, can meet gas-based shaft kiln directly reduced iron-smelting process requirement.CO2After trapping
The calorific value of pyrolysis gas rises to 5152Kcal/Nm3, it is greatly improved the utilization of pyrolysis gas.
Accompanying drawing explanation
Fig. 1 is the method flow schematic diagram that the present invention prepares high concentration CO with rubbish charcoal for raw material.
Detailed description of the invention
Below in conjunction with drawings and Examples, the detailed description of the invention of the present invention is carried out more detailed theory
Bright, so as to the advantage being more fully understood that the solution of the present invention and various aspects.But, below
The detailed description of the invention and the embodiment that describe are only descriptive purpose rather than limitation of the present invention.
As it is shown in figure 1, the method that the present invention prepares high concentration CO with rubbish charcoal for raw material includes life
Rubbish pretreatment, refuse pyrolysis, broken pyrolytic carbon, the energy-conservation deacidification of pyrolysis oil gas and isolation of purified,
CO2The steps such as trapping and fluidized-bed gasification furnace gasification.
House refuse pretreatment is that rubbish sequentially passes through broken bag, roller screen, sorting and break process, will
Bulk inorganic matter therein, metal etc. separates and is crushed to pan feeding requirement, the pretreated rubbish of rubbish
The particle diameter ＜ 20mm of raw material, the moisture content of described garbage raw material is 20%-60%.
In refuse pyrolysis step, garbage raw material uniformly being sent into revolving bed pyrolysis oven, layer thickness is
50-250mm, heats up through the stage in stove, through being dried, being pyrolyzed and priming reaction, response time
(time that i.e. revolving bed rotates a circle) is about 1h, and the material obtained includes pyrolytic carbon, pyrolysis oil gas.
Pyrolytic carbon is through crusher in crushing, the particle diameter ＜ 10mm of pyrolytic carbon.500 DEG C of pyrolysis oil gas are through pipeline
Entering energy-conservation deacidifying device and complete waste heat recovery and deacidification, temperature is down to 350 DEG C, and acidic gas concentration drops
To 0.05%.Utilize reclaim waste heat noble gas is preheated, preheating temperature up to about 210 DEG C,
Noble gas after preheating sends into drying process, can be to house refuse raw material, percolate and pyrolysis sewage
Etc. be evaporated concentrate, it is achieved noble gas recycles.
Pyrolysis oil gas after process enters Oil-gas Separation purifier and realizes the separation of oil gas, pyrolysis gas
Dedusting, desulphurization and denitration etc..Specifically, in wet dedusting tower, the spray of Quench recirculated water is first used
Spilling pyrolysis oil gas, it is achieved dedusting and pyrolysis oil, the separation of pyrolysis gas, pyrolysis gas enters transverse pipe initial cooler,
Pyrolysis gas is cooled to 21 DEG C of left sides by primary cooler two sections of cooling water of 32 DEG C of recirculated waters and 16 DEG C of chilled water
Right.The pyrolysis gas discharged by primary cooler bottom enters the electrical tar precipitator that two parallel connections operate simultaneously, complete
Become the tar work carried secretly in gas.By Roots blower, pyrolysis gas is delivered to desulphurization denitration tower again, complete
Become desulphurization denitration, produce pure pyrolysis gas.
CO2In trapping step, the pyrolysis gas after Oil-gas Separation purifies feeds absorption tower through blower fan pressurization,
With absorbent counter current contacting in absorption tower, use alkanolamine solution as absorbent, the CO in pyrolysis gas2
Being absorbed by absorbent, become rich solution, rich solution feeds desorber through rich solution pump, and desorbing generates CO2Gas,
Steam and the mixed gas of mist and lean solution；CO after desorbing2Cooled device carries out cooling down, steam
Water and foam is become with mist；Mixed gas after cooling enters gas-liquid separator, removes mixed gas
Interior water and foam, isolated CO2Gas enters fluidized-bed gasification furnace as gasifying agent.
Fluidized-bed gasification furnace gasifies: as the CO of gasifying agent2With the broken rear pyrolytic carbon as gasified raw material
Entering described fluidized-bed gasification furnace to gasify, the gasification temperature of fluidized-bed gasification furnace is about 1000 DEG C,
Produce gasification gas CO.Part gasification gas CO is as the reduction in gas-based shaft kiln directly reduced iron-smelting process
Agent, part gasification gas CO is as the supplementary fuel of radial canal.
In fluidized-bed gasification furnace gasification step, the gas CO that gasifies described in a part for generation erects through gas base
Stove processes, the CO of generation2Gas sends into described fluidized-bed gasification furnace；Gasify described in another part gas CO
Send into described revolving bed pyrolysis oven.
Gas-based shaft kiln comprises reduction section and cooling section, during gas-based shaft kiln reduction iron production, and fluidisation
Bed gasification furnace gasification produce high concentration CO be delivered in gas-based shaft kiln from cooling section, in order to make CO with
Sponge iron in cooling section enters reduction section after carrying out heat exchange and carries out reduction reaction, and CO is through hot sponge
After ferrum preheating, temperature reaches more than 850 DEG C, can directly carry out reduction reaction, reduces the reaction of reduction section
Temperature, energy consumption reduces.CO after preheating ascends into reduction section, and reverse with the acid pellet fallen
There is reduction reaction in contact, generates high-temperature sponge iron and high concentration CO2, CO2Discharged also by top gas outlet
Entering fluidized gasification bed to use as gasifying agent, this process achieves CO2Recycle, reduce carbon row
High-volume.
It is specifically described below and realizes above-mentioned preparing high concentration CO method with rubbish charcoal for raw material in the present invention
System.
According to processing technological requirement, rubbish pretreatment unit is by broken bag mechanism, roller screen mechanism, separator
Structure and crushing mechanism are sequentially connected with composition, and described mechanism is respectively provided with charging aperture and discharging opening；
Revolving bed pyrolysis oven is by dry section, pyrolytic reaction one district, pyrolytic reaction two district and pyrolytic reaction three
District is constituted, and the top in each district has pyrolysis oil gas vent, the radial canal in each district to have gas inlet；
The front end of dry section has garbage raw material entrance, the end in described pyrolytic reaction three district to have pyrolytic carbon discharging opening；
Radial canal is the heater of revolving bed pyrolysis oven, and it is revolving bed pyrolysis oven heat supply by burning.
The charging aperture of disintegrating machine is connected with pyrolytic carbon discharging opening, the storage charcoal groove outlet of disintegrating machine and fluid bed
The pyrolytic carbon charging aperture of gasification furnace is connected；
Revolving bed pyrolysis oven, energy-saving denitration device, Oil-gas Separation purifier, CO2Capturing device, stream
Change bed gasification furnace to be sequentially connected with.
Further, energy-saving denitration device includes noble gas air accumulator, inert gas duct, pyrolysis
Oil and gas pipes, deacidification-accumulation of heat complex, wherein pyrolysis oil gas air inlet and the pyrolysis of revolving bed pyrolysis oven
Oil gas vent is connected.
Oil-gas Separation purifier is by oil pyrolysis gas pipeline, wet dedusting tower, primary cooler, electrically trapped tar oil
Device, aerator, desulfurizing tower, denitrating tower are sequentially connected with composition, and oil pyrolysis gas conduit air inlet is with energy-conservation
The pyrolysis oil gas vent of denitrification apparatus is connected；Gas wash tower has air inlet and gas outlet, gas wash tower air inlet
Being connected with pyrolysis oil feed channel gas outlet, gas wash tower gas outlet is connected with desulfurizing tower air inlet, desulfurizing tower
Gas outlet is connected with denitrating tower air inlet.
CO2Capturing device is by absorption tower, rich solution pump, desorber, reboiler, gas-liquid separator, lean solution
Pump and lean solution cooler are sequentially connected with composition；The air inlet on absorption tower and the denitrating tower of energy-saving denitration device
Gas outlet be connected, the gas outlet of gas-liquid separator and the CO of fluidized-bed gasification furnace2Air inlet is connected.
Specifically, the entrance of rich solution pump is connected with absorption tower the second outlet bottom absorption tower；Rich solution pump
Outlet be connected with desorber first entrance on described desorber top；The entrance of lean pump and described solution
The desorber first inhaling tower bottom exports connected；Desorber bottom the entrance of reboiler and desorber the
Two outlets are connected, and the outlet of desorber the second entrance and reboiler is connected, the desorber at desorber top the
Gas-liquid separator entrance described in three outlet, lean pump outlet is connected with the entrance of lean solution cooler.
Fluidized-bed gasification furnace gasification furnace is rubbish charcoal gasification installation, has CO2Air inlet, pyrolytic carbon feed
Mouth, CO outlet and gasification solid discharge, CO outlet is connected with air accumulator air inlet, and pyrolytic carbon feeds
Mouth is connected with storage charcoal groove outlet.
In air accumulator, air inlet exports with the CO of fluidized-bed gasification furnace and is connected, and the first of air accumulator goes out
QI KOU is connected with the gas inlet of revolving bed pyrolysis oven, the second gas outlet of air accumulator and gas-based shaft kiln
It is connected.
Gas-based shaft kiln is provided with charging aperture, discharge gate, reducing gases entrance and top gas outlet, and top gas goes out
Mouth is connected with the CO2 air inlet of fluidized-bed gasification furnace, and gas-based shaft kiln has reduction chamber and is positioned at reduction
Cooling chamber below chamber, wherein, described reduction chamber has reducing gases import, cooling chamber cold
But gas import is connected with the second gas outlet of air accumulator.
Embodiment
Using certain city's house refuse is raw material, and material composition composition is shown in Table 1 below.
Table 1 house refuse becomes to be grouped into (wt%)
The rubbish entering factory removes bulk inorganic matter and metal through simple sorting, then crushes, broken
The broken refuse pyrolysis raw material particle size ＜ 20mm obtained；
Broken rubbish is uniformly fed revolving bed pyrolysis oven, fabric thickness 100mm, in stove rubbish with
Furnace bottom to rotate through dry section, pyrolytic reaction one district, pyrolytic reaction two district and pyrolytic reaction three district complete
Become pyrolytic reaction, wherein dry section temperature 350 DEG C, pyrolytic reaction one district, pyrolytic reaction two district and pyrolysis
React three district's temperature 800 DEG C, response time 2-3h.
House refuse through pyrolysis oven be pyrolyzed after pyrolysis gas composition and calorific value be shown in Table 2 below.Heat
Vent one's spleen middle CO2Content is 28%, gas heating value 3962Kcal/Nm3。
Table 2 pyrolysis gas composition and calorific value
Through CO2After capturing device processes, CO2The response rate is up to more than 90%, and purity is up to more than 98%.
High-purity CO2Carrying out gasification reaction with rubbish charcoal at normal pressure, at 1200 DEG C, charcoal conversion ratio reaches more than 97%.
In gasification gas, CO purity reaches more than 98%, can meet gas-based shaft kiln directly reduced iron-smelting process requirement.Catch
Collection CO2After pyrolysis gas character be shown in Table 3 below.The calorific value of pyrolysis gas is by 3962Kcal/Nm3Rise to
5152Kcal/Nm3, improve the utilization ways of pyrolysis gas.
Table 3 pyrolysis gas composition and calorific value
Domestic garbage pyrolysis produces substantial amounts of pyrolysis gas, is the primary product of pyrolysis generation economic worth,
But owing to wherein containing the CO of about 30%2, pyrolysis gas calorific value is relatively low, restricts its use approach, reduces
The economic benefit of Prediction for Solid Waste Treatment Technology, makes the promotion and application of pyrolytic technique receive limit greatly
System.The CO that the present invention uses2Trapping technique separates and collects CO2, improve the calorific value of pyrolysis gas, after collection
CO2High concentration CO can be prepared, it is achieved CO as gasifying agent2Recycling, reduces carbon emission amount,
Improve environmental benefit.
There is the poisonous and harmful substances such as heavy metal in rubbish charcoal, calorific value is low, and market outlet is poor, if made
Using for solid fuel, combustion efficiency is poor, and can produce substantial amounts of secondary pollution in combustion process,
Environmental benefit is poor, and the most most of rubbish charcoals carry out landfill disposal only as pyrolysis residue, take
Land resource and cause the waste of the energy, the present invention uses gasification technology that rubbish charcoal is made high concentration CO,
Can increase economic efficiency, simultaneously the high concentration of output as gas-based shaft kiln directly reduced ironmaking reducing agent
CO2Fluidized-bed gasification furnace is returned, it is achieved CO as gasifying agent2Inner loop utilizes, and makes house refuse heat
Solution technology all has huge competitiveness in terms of economy and the feature of environmental protection, is greatly promoted Technique Popularizing
And application.
Last it is noted that obvious, above-described embodiment is only by clearly demonstrating what the present invention was made
Citing, and not restriction to embodiment.For those of ordinary skill in the field, exist
Can also make other changes in different forms on the basis of described above.Here without also without
All of embodiment is given exhaustive by method.And the obvious change thus amplified out or variation
Among protection scope of the present invention.
Claims (10)
1. the method preparing high concentration CO with rubbish charcoal for raw material, it comprises the following steps:
Pretreatment: rubbish sequentially passes through broken bag, roller screen, sorting and break process, obtains garbage raw material；
Refuse pyrolysis: send into the described garbage raw material of revolving bed pyrolysis oven through being dried, be pyrolyzed and activating
Reaction, the material obtained includes pyrolytic carbon, pyrolysis oil gas；
Broken pyrolytic carbon: through the described pyrolytic carbon particle diameter ＜ 10mm of crusher in crushing；
Energy-conservation deacidification and isolation of purified: described pyrolysis oil gas is clean through energy-conservation deacidifying device and Oil-gas Separation
Gasifying device processes, and obtains pyrolysis gas；
CO2Trapping: described pyrolysis gas is through CO2Capturing device processes, and isolates CO2Gas；
Fluidized-bed gasification furnace gasify: described in isolate CO2Described stream is entered with the described pyrolytic carbon after broken
Change bed gasification furnace to gasify, produce gasification gas CO.
Method the most according to claim 1, it is characterised in that described pyrolysis gas enters CO2Catch
The absorption tower of acquisition means, contacts with alkanolamine solution in absorption tower, the CO in described pyrolysis gas2Described
Alkanolamine solution absorbs and becomes rich solution, and described rich solution is pumped into desorber through rich solution, the mixing after desorbing
Gas and lean solution cooled device cooling down, the mixed gas after cooling enters gas-liquid separator, separates
Go out CO2Gas.
Method the most according to claim 1, it is characterised in that a part of described gasification gas CO
As the reducing agent of gas-based shaft kiln reduction iron production, the CO of generation2Gas sends into described fluidized-bed gasification furnace；
The gas CO that gasifies described in another part sends into described revolving bed pyrolysis oven.
Method the most according to claim 1, it is characterised in that described pyrolysis oil gas is by described
After the process of energy-conservation deacidification, the temperature of described pyrolysis oil gas is down to 250 DEG C-350 DEG C, sour gas volume
Concentration 0.05%；Wet dedusting tower in described Oil-gas Separation purifier uses 70-80 DEG C of Quench to follow
Ring water sprays described pyrolysis oil gas, it is achieved dedusting and pyrolysis oil, the separation of pyrolysis gas, the institute after dedusting
State pyrolysis gas to cool down in primary cooler, be then fed into detar in electrical tar precipitator, then will by aerator
Pyrolysis gas delivers to desulfurizing tower and denitrating tower, produces pure pyrolysis gas；Described primary cooler recirculated water and
Chilled water is by described pyrolysis oil air cooling to 20-25 DEG C, and the temperature of described recirculated water and described chilled water is divided
Wei 30-35 DEG C and 15-20 DEG C.
Method the most according to claim 1, it is characterised in that the particle diameter ＜ of described garbage raw material
20mm, the moisture content of described garbage raw material is 20%-60%；In described revolving bed pyrolysis oven, described rubbish
Rubbish raw material layer thickness is 50-250mm；The gasification temperature of fluidized-bed gasification furnace is 900-1100 DEG C.
6. realize a system for the described method of one of claim 1 to 5, comprising:
Rubbish pretreatment unit: by broken bag mechanism, roller screen mechanism, sorting mechanism and crushing mechanism successively
Connecting and composing, described mechanism is respectively provided with charging aperture and discharging opening；
Revolving bed pyrolysis oven: by dry section, pyrolytic reaction one district, pyrolytic reaction two district and pyrolytic reaction
3rd district are constituted, and the top in each described district has pyrolysis oil gas vent, the radial canal in each described district to have combustion
Gas air inlet；There are garbage raw material entrance, the end in described pyrolytic reaction three district in the front end of described dry section
There is pyrolytic carbon discharging opening；
The charging aperture of disintegrating machine is connected with described pyrolytic carbon discharging opening, the storage charcoal groove outlet of described disintegrating machine
It is connected with the pyrolytic carbon charging aperture of fluidized-bed gasification furnace；
Described revolving bed pyrolysis oven, energy-saving denitration device, Oil-gas Separation purifier, CO2Capturing device
It is sequentially connected with described fluidized-bed gasification furnace.
System the most according to claim 6, it is characterised in that the heat of described energy-saving denitration device
Solve oil gas air inlet to be connected with the pyrolysis oil gas vent of described revolving bed pyrolysis oven；
Described Oil-gas Separation purifier is by oil pyrolysis gas pipeline, wet dedusting tower, primary cooler, electric fishing
Tar device, aerator, desulfurizing tower, denitrating tower are sequentially connected with composition；Described oil pyrolysis gas pipeline and institute
The pyrolysis oil gas vent stating energy-saving denitration device is connected.
System the most according to claim 7, it is characterised in that described CO2Capturing device is by inhaling
Receive tower, rich solution pump, desorber, reboiler, gas-liquid separator, lean pump and lean solution cooler successively
Connect and compose；The gas outlet phase of the air inlet on described absorption tower and the denitrating tower of described energy-saving denitration device
Even, the gas outlet of described gas-liquid separator is connected with the air intake of described fluidized-bed gasification furnace.
System the most according to claim 8, it is characterised in that the entrance of described rich solution pump and institute
State the absorption tower second bottom absorption tower and export connected；On described rich solution delivery side of pump and described desorber
Desorber first entrance in portion is connected；Desorber bottom the entrance of described lean pump and described desorber
First outlet is connected；Desorber second bottom the entrance of described reboiler and described desorber exports phase
Even, described desorber the second entrance is connected with the outlet of described reboiler, the desorbing at described desorber top
Gas-liquid separator entrance described in tower the 3rd outlet, the outlet of described lean pump and described lean solution cooler
Entrance be connected.
System the most according to claim 9, it is characterised in that the air inlet of air accumulator and institute
The gasification gas outlet stating fluidized-bed gasification furnace is connected, the first gas outlet of described air accumulator and described rotation
The gas inlet of bed pyrolysis oven is connected, and the second gas outlet of described air accumulator is connected with gas-based shaft kiln.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106521069A (en) * | 2016-12-14 | 2017-03-22 | 北京神雾环境能源科技集团股份有限公司 | System and method for coupling reduction ironmaking of garbage disposal |
| CN106642134A (en) * | 2016-11-29 | 2017-05-10 | 北京神雾环境能源科技集团股份有限公司 | Method and system for combined treatment of household rubbish and fly ash |
| CN108753330A (en) * | 2018-08-14 | 2018-11-06 | 李新方 | A kind of industry combustiblerefuse carbonization-pyrolysis oven and total system |
| CN110591765A (en) * | 2019-08-05 | 2019-12-20 | 浙江骐骥环境科技有限公司 | RDF pyrolysis gas noncondensable gas clean system |
| CN113559796A (en) * | 2021-07-01 | 2021-10-29 | 河北科技大学 | Coupling type coal powder pyrolysis and semicoke reduction CO2Apparatus and method for producing CO |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1462505A1 (en) * | 1994-12-01 | 2004-09-29 | Mitsubishi Jukogyo Kabushiki Kaisha | Fixed-bed gasification furnaces and methods for gasifying organic waste |
| CN101314102A (en) * | 2008-05-30 | 2008-12-03 | 西安热工研究院有限公司 | Method and apparatus for collecting carbonic anhydride in coal-fired plant flue gas |
| CN102994678A (en) * | 2012-11-21 | 2013-03-27 | 北京神雾环境能源科技集团股份有限公司 | Method and system for pulverized coal gasification for gas generation and direct reduction metallurgy of gas-based shaft furnace |
| CN203269882U (en) * | 2013-04-07 | 2013-11-06 | 邢力 | Pyrolysis catalysis gasifier for domestic garbage |
| CN104084031A (en) * | 2014-06-06 | 2014-10-08 | 山西玉竹活性石灰制造有限公司 | A flue gas purification device of a lime shaft kiln adopting soft coal as fuel |
| CN104804775A (en) * | 2015-04-20 | 2015-07-29 | 北京神雾环境能源科技集团股份有限公司 | Method and system for producing combustible gas from domestic waste through pyrolysis gasification |
-
2016
- 2016-06-08 CN CN201610406051.3A patent/CN105861072A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1462505A1 (en) * | 1994-12-01 | 2004-09-29 | Mitsubishi Jukogyo Kabushiki Kaisha | Fixed-bed gasification furnaces and methods for gasifying organic waste |
| CN101314102A (en) * | 2008-05-30 | 2008-12-03 | 西安热工研究院有限公司 | Method and apparatus for collecting carbonic anhydride in coal-fired plant flue gas |
| CN102994678A (en) * | 2012-11-21 | 2013-03-27 | 北京神雾环境能源科技集团股份有限公司 | Method and system for pulverized coal gasification for gas generation and direct reduction metallurgy of gas-based shaft furnace |
| CN203269882U (en) * | 2013-04-07 | 2013-11-06 | 邢力 | Pyrolysis catalysis gasifier for domestic garbage |
| CN104084031A (en) * | 2014-06-06 | 2014-10-08 | 山西玉竹活性石灰制造有限公司 | A flue gas purification device of a lime shaft kiln adopting soft coal as fuel |
| CN104804775A (en) * | 2015-04-20 | 2015-07-29 | 北京神雾环境能源科技集团股份有限公司 | Method and system for producing combustible gas from domestic waste through pyrolysis gasification |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106642134A (en) * | 2016-11-29 | 2017-05-10 | 北京神雾环境能源科技集团股份有限公司 | Method and system for combined treatment of household rubbish and fly ash |
| CN106521069A (en) * | 2016-12-14 | 2017-03-22 | 北京神雾环境能源科技集团股份有限公司 | System and method for coupling reduction ironmaking of garbage disposal |
| CN108753330A (en) * | 2018-08-14 | 2018-11-06 | 李新方 | A kind of industry combustiblerefuse carbonization-pyrolysis oven and total system |
| CN110591765A (en) * | 2019-08-05 | 2019-12-20 | 浙江骐骥环境科技有限公司 | RDF pyrolysis gas noncondensable gas clean system |
| CN113559796A (en) * | 2021-07-01 | 2021-10-29 | 河北科技大学 | Coupling type coal powder pyrolysis and semicoke reduction CO2Apparatus and method for producing CO |
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