CN110129077A - Pyrolytic process - Google Patents
Pyrolytic process Download PDFInfo
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- CN110129077A CN110129077A CN201910345225.3A CN201910345225A CN110129077A CN 110129077 A CN110129077 A CN 110129077A CN 201910345225 A CN201910345225 A CN 201910345225A CN 110129077 A CN110129077 A CN 110129077A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/34—Regenerating or reactivating
- B01J20/3416—Regenerating or reactivating of sorbents or filter aids comprising free carbon, e.g. activated carbon
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/34—Regenerating or reactivating
- B01J20/3483—Regenerating or reactivating by thermal treatment not covered by groups B01J20/3441 - B01J20/3475, e.g. by heating or cooling
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- 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
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- 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
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- 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
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
- C10B57/10—Drying
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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
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/20—Apparatus; Plants
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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
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/86—Other features combined with waste-heat boilers
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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
- 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
-
- 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
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Combustion & Propulsion (AREA)
- Analytical Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Processing Of Solid Wastes (AREA)
- Gasification And Melting Of Waste (AREA)
Abstract
The present invention provides a kind of pyrolytic process, including desiccation pretreatment；Organic dangerous waste is pyrolyzed to obtain the first thermal decomposition product；It provides the first separator to separate the first thermal decomposition product, obtains pyrolysis gas and residue；Pyrolysis gas burning generates high-temperature flue gas, and high-temperature flue gas enters the first pyrolysis installation and provides heat source for it；Waste active carbon pyrolysis generates the second thermal decomposition product；The second separator is provided to enter in combustion chamber the isolated desorption gas of the second thermal decomposition product and regenerated carbon, desorption gas；High-temperature flue gas into the first pyrolysis installation provides heat source for the second pyrolysis installation, enters back into waste heat boiler, and heats the generation saturated steam of the water in waste heat boiler and provide heat source for desiccation apparatus.The pyrolysis gas burning that pyrolytic process of the present invention generates generates high-temperature flue gas, is followed successively by organic dangerous waste pyrolysis, Regenevating Waste Activated Carbon and waste heat boiler and provides heat source, the saturated steam that waste heat boiler generates provides heat source again for anhydration system, forms recycling for resource.
Description
Technical field
The present invention relates to the utilization of resources fields of organic dangerous waste, more particularly to the pyrolytic process of organic dangerous waste.
Background technique
Under the modernized big insutry background of high concentration, the organic hazardous waste of industrial production discharge is to ambient enviroment
Pollution get worse, it will directly seriously affect fishery and agricultural generation, while directly or indirectly be detrimental to health.
The pollution effect of organic hazardous waste is so big, but is but in blank for organic dangerous waste disposal.
The enterprises and institutions such as numerous petrochemical industries, electronics processing, fine chemistry industry, pharmacy, machine-building and environment protection treating are every
Generate a large amount of organic hazardous waste year, on the one hand these enterprises and institutions can not find the receiving unit of hazardous waste, even if
Large-scale disposition unit can be found, the problems such as quantity is not concentrated, storage package is lack of standardization, disposal costs are high is also faced with；Another party
Face, environmental management department are also faced with the problem for producing that useless unit is more, distribution is wide, hazardous waste is wide in variety, total amount is big, the difficulty of management
Degree is very big.
By taking pharmaceutical factory as an example, China is the country that the remaining pharmacy dregs of a decoction are most in the world, and qualitative from the dregs of a decoction in 2008 is dangerous waste
Since, annual a large amount of dregs of a decoction remainings.The dregs of a decoction are pharmaceutical industry raw materials containing pharmacological property after the processes effective component extracting such as boiling, fermentation
Residual residue, mainly have Chinese medicine residue and antibiotic residue；The useless dregs of a decoction mainly contain the nutritional ingredients such as crude protein, sugar and lack
Remaining antibiotic is measured, easily fermentation is rotten distributes foul odour, moisture content height (90% or more), it is difficult to dispose.It is how safe
The effectively large-scale useless dregs of a decoction of disposition, have been the great difficult problems that current China's pharmacy faces.
Active carbon is commonly used due to having very big specific surface, multi-functional adsorption potential and surface chemical structure abundant simultaneously
Come the Adsorption of Organic removal or decolorization of drug and pharmacy waste water；Therefore the dregs of a decoction and waste active carbon are that pharmaceutical factory generates
Measure maximum two classes dangerous waste object.
It is reported that the processing method of pharmacy waste residue mainly includes anaerobic digestion, aerobic compost, burning etc. at present, but due to medicine
Slag antibiosis, infectivity and easy diffusivity, all there are certain drawbacks in digestion and composting mode, and common burning disposal work
Skill, since the particularity and moisture content of its ingredient are high, processing cost per ton reaches 2000 yuan or more, some environmental requirements compared with
High industrial park, the cost of burning disposal is even as high as 4000 yuan/ton or more, so that pharmacy corporation generally faces " can not burning "
Predicament.Although anaerobic digestion methane production centainly depth can generate stench during the fermentation and be difficult to press down using the useless dregs of a decoction
System, and water disposing technique is complicated, it is at high cost.
Pollutant emission can be preferably controlled using the pyrolytic gasification technical treatment dregs of a decoction, controls processing cost.The technology
Be under the hot conditions of anaerobic or anoxic, make the larger molecular organics in the dregs of a decoction be cracked into flammable micro-molecular gas (H2,
CH4 and CO etc.), the methanol of liquid, acetone, acetic acid, acetaldehyde, tar, solvent naphtha and fixed carbon (coke, carbon black) etc., small molecule
Substance can burn or collect, residue landfill disposal.
Such as the CN109161563A patent of Tsinghua University discloses a kind of pyrolysis treating method of antibiotic dregs of a decoction, adopts
Waste water in the dregs of a decoction is separated with the mode of hydro-thermal filters pressing, and is pyrolyzed using dregs of a decoction anoxybiotic, the technique of wastewater anaerobic digestive keeps its harmless
Change and recycling.The hydrothermal pretreatment antibiotic dregs of a decoction can reduce dregs of a decoction desiccation cost, but thus a large amount of waste water of bring are but
It is difficult to handle, anaerobic digestion effect is more general, and the processing of carbon residue gasification and tail gas is not implemented in technique.In addition, due to nothing
In oxygen pyrolytic process, moisture contained in the biomass garbages such as dregs of a decoction evaporation need to consume a large amount of energy, meanwhile, to the dregs of a decoction into
When the processing of row Non-oxygen pyrolytic, temperature usually requires to reach 500 DEG C~650 DEG C, therefore the flue-gas temperature discharged is also high, causes a large amount of
Heat loss become Non-oxygen pyrolytic processing biomass so that high using the operating cost of Non-oxygen pyrolytic method processing biomass garbage
Rubbish Technique Popularizing, application major obstacle.
Active carbon higher cost, directly burning will cause a large amount of energy waste, no matter from economic benefit or from environmental protection
Angle considers that it is all very necessary for carrying out the regeneration of active carbon.For Regenevating Waste Activated Carbon, at present prevailing technology be heat treatment and
Gasify method of reproduction, for example patent CN108178353A describes a kind of technical method that antibiotic bacterium Slag treatment utilizes, and utilizes heat
Desorption and steam gasification boring technique make active carbon activity recovery, and patent CN107913689A discloses a kind of dangerous waste solid waste again
The method of liveliness proof charcoal, using flash distillation desiccation, elevated temperature desorption, CO2 and vapor pore-creating mode activity recovery carbon activity.However,
The cost of above method regenerated carbon is high.
In conclusion in the prior art, the thermal energy consumption generated after being pyrolyzed to organic dangerous waste such as the dregs of a decoction is very big, but without
Method makes the organic matter in organic dangerous waste such as dregs of a decoction be converted into storage characteristics resource, cannot achieve the resource utilization of organic dangerous waste, and
The cost of regenerated carbon is again very high simultaneously, it is therefore necessary to invent a kind of new pyrolytic process.
Summary of the invention
In order to overcome shortcoming and defect existing in the prior art, may be implemented to provide the purpose of the present invention is to provide one kind
The pyrolytic process that source recycles.
For achieving the above object, the present invention uses following pyrolytic processes:
S1: desiccation apparatus is provided, desiccation pretreatment is carried out to organic dangerous waste to be processed；S2: have desiccation is pretreated
Machine dangerous waste is sent into the first pyrolysis installation and carries out pyrolysis processing, and pyrolysis obtains the first thermal decomposition product；S3: the first separator pair is provided
First thermal decomposition product is separated, and pyrolysis gas and residue are respectively obtained；S4: providing combustion chamber, and combustion chamber and first are separated
Device is connected, and pyrolysis gas enters combustion chamber from the first separator, and pyrolysis gas burns in the combustion chamber and generates high temperature cigarette
Gas, high-temperature flue gas enter the first pyrolysis installation from combustion chamber and provide heat source for the first pyrolysis installation；S5: by useless activity to be processed
Charcoal is sent into the second pyrolysis installation, and the second pyrolysis installation carries out pyrolysis processing to waste active carbon and generates the second thermal decomposition product；S6: it provides
Second separator carries out isolated desorption gas to the second thermal decomposition product and regenerated carbon, desorption gas enter combustion chamber
It is interior；S7: waste heat boiler is connected with the first pyrolysis installation and the second pyrolysis installation, into the first pyrolysis installation high-temperature flue gas from
First pyrolysis installation enters the second pyrolysis installation and provides heat source for the second pyrolysis installation, into the high-temperature flue gas of the second pyrolysis installation
Enter in waste heat boiler from the second pyrolysis installation, and heats the generation saturated steam of the water in waste heat boiler and provided for desiccation apparatus
Heat source.
Organic dangerous waste of pyrolytic process of the present invention carries out the pyrolysis processing of organic dangerous waste, organic dangerous waste after desiccation pre-processes
The pyrolysis gas generated in pyrolytic process enters burning Indoor Combustion and generates high-temperature flue gas, is followed successively by the pyrolysis of organic dangerous waste
Processing, the regeneration of waste active carbon and waste heat boiler provide heat source, and the saturated steam that waste heat boiler generates mentions again for anhydration system
Supplying heat source forms recycling for resource.
Pyrolytic process of the invention in the regenerative process of the minimizing of organic dangerous waste, harmless treatment and waste active carbon,
The cycling and reutilization of resource is utmostly realized, while organic dangerous waste processing system and Regenevating Waste Activated Carbon system is integrated
Change, saves equipment investment, greatly improve the treatment effeciency of Chan Fei enterprise.
Detailed description of the invention
Fig. 1 is the structural block diagram of pyrolysis system of the present invention.
Fig. 2 is the flow chart of pyrolytic process of the present invention.
Appended drawing reference
11 flue gas purification system 100 of desiccation apparatus
Organic 200 regenerating active carbon system 300 of dangerous waste processing system
First feeding warehouse, 21 second feeding warehouse 31
First helical feed screw rod, 22 second helical feed screw rod 32
First pyrolysis installation, 23 second pyrolysis installation 33
First separator, 24 second separator 34
26 collection device 36 of combustion chamber
261 denitrification apparatus 27 of auxiliary burner
13 dust-extraction unit 14 of waste heat boiler
15 smoke discharging device 16 of deacidifying device
51 second switch valve 52 of first switch valve
Third switch valve 53
Specific embodiment
In order to make the objectives, technical solutions, and advantages of the present invention clearer, with reference to the accompanying drawings and embodiments, right
The present invention is further elaborated.It should be appreciated that the specific embodiments described herein are merely illustrative of the present invention, and
It is not used in the restriction present invention.
The pyrolysis system that pyrolytic process of the invention uses is for handling organic dangerous waste and waste active carbon, such as Fig. 1
It is shown, pyrolysis system of the invention include desiccation apparatus 11, organic dangerous waste processing system 200, Regenevating Waste Activated Carbon system 300,
Waste heat boiler 13 and flue gas purification system 100.
Desiccation apparatus 11 carries out drying and other treatment to organic dangerous waste to be processed, for reducing the moisture content of organic dangerous waste.
Fig. 1 is please referred to, organic dangerous waste processing system 200 includes the first feeding warehouse 21, the first helical feed screw rod 22, first
Pyrolysis installation 23, the first separator 24, combustion chamber 26 and denitrification apparatus 27.First feeding warehouse 21 is connected with desiccation apparatus 11,
First helical feed screw rod 22 is set between the first feeding warehouse 21 and the first pyrolysis installation 23.First pyrolysis installation 33 includes the
One pyrolysis chamber (not shown) and the first thermal decomposition tube (not shown) being located in the first pyrolysis chamber (not shown).
Regenevating Waste Activated Carbon system 300 includes the second feeding warehouse 31 and the second helical feed screw rod 32, the second pyrolysis installation
33, the first separator 34 and collection device 36, the second helical feed screw rod 32 are set to the second feeding warehouse 31 and the second pyrolysis
Between device 33.Second pyrolysis installation 33 include the second pyrolysis chamber (not shown) and be located in the second pyrolysis chamber (not shown) the
Two thermal decomposition tubes (not shown).
Flue gas purification system 100 includes dust-extraction unit 14, deacidifying device 15 and smoke discharging device 16, and dust-extraction unit 14 connects
Pass to the exhanst gas outlet (not indicating) of waste heat boiler 13.
Referring to Fig. 2, pyrolytic process of the invention carries out pyrolysis processing to organic dangerous waste and waste active carbon carries out again
It is raw, pyrolytic process of the invention include desiccation pretreatment, the pyrolysis processing of organic dangerous waste, the regeneration of waste active carbon, UTILIZATION OF VESIDUAL HEAT IN,
Fume treatment and etc., detailed description are as follows for the step:
A. desiccation pre-processes
S1: desiccation apparatus 11 is provided, organic dangerous waste to be processed is pre-processed；
In this step, the pretreated organic dangerous waste moisture content of desiccation is between 5% to 30%, it is preferable that organic danger
Useless moisture control is between 10% to 20%.The moisture content of organic dangerous waste is too high, will affect the pyrolysis effect of organic dangerous waste
With the burning of pyrolysis gas in the combustion chamber, moisture content is too low, will affect the fixation gasification reaction in organic dangerous waste, thus shadow
Ring the minimizing of organic dangerous waste.
B. the pyrolysis processing of organic dangerous waste
S2: the pretreated organic dangerous waste of desiccation is sent into the first pyrolysis installation 23 and carries out pyrolysis processing, pyrolysis obtains
First thermal decomposition product；
In the present embodiment, the pretreated organic dangerous waste of desiccation is transmitted to the first feeding warehouse via conveyer belt (not shown)
21, then be conveyed into the first thermal decomposition tube (not shown) via the first helical feed screw rod 22 from the first feeding warehouse 21.
Maximum temperature and organic dangerous waste in the present embodiment, in the first thermal decomposition tube (not shown) of the first pyrolysis installation 23
Residence time in the first thermal decomposition tube (not shown) of the first pyrolysis installation 23, not according to the ingredient of organic dangerous waste, treating capacity
Different from together, it is preferable that the first thermal decomposition tube (not shown) interior maximum temperature of the first pyrolysis installation 23 is at 600 DEG C to 950
Between DEG C, residence time of organic dangerous waste in the first thermal decomposition tube (not shown) of the first pyrolysis installation 23 is 5 to 30 minutes, should
The pyrolysis processing process of organic dangerous waste includes: in step S2
A. it drying stage: dries organic dangerous waste and generates vapor；
B. pyrolysis phase: the organic cracking of macromolecular is small molecule compound and carbon residue in organic dangerous waste；
C. gasifying stage: the vapor that carbon residue is generated with drying stage reacts, and generates pyrolysis gas.
S3: the first separator 24 is provided, the first thermal decomposition product is separated, respectively obtain pyrolysis gas and residue；It is residual
Slag is drawn via the first deslagging spiral (not shown) from 25 bottom of the first separator.
S4: providing combustion chamber 26, combustion chamber 26 be connected with the first separator 24, and pyrolysis gas is from the first separator
24 enter combustion chamber 26, and pyrolysis gas burns in combustion chamber 26 and generates high-temperature flue gas, and high-temperature flue gas enters from combustion chamber 26
First pyrolysis installation 23 is that the first pyrolysis installation 23 provides heat source；
In the present embodiment, combustion chamber 26 further comprises the input end that combustion chamber 26 is arranged in auxiliary burner 261, auxiliary
Burner 261 sprays into combustion gas into combustion chamber 26 by temperature control feedback, to adjust the temperature in combustion chamber 26, it is preferable that
Temperature in combustion chamber 26 controls between 850 DEG C to 1200 DEG C, it is preferable that temperature controls as 1100 DEG C extremely in combustion chamber 26
1150℃.Flue gas residence time in combustion chamber 26 is no less than 2 seconds, and the burning in combustion chamber 26 is low nitrogen burning.
C. the pyrolysis regeneration of waste active carbon:
S5: waste active carbon to be processed is sent into the second pyrolysis installation 33, the second pyrolysis installation 33 to waste active carbon into
Row pyrolysis processing generates the second thermal decomposition product；
In the present embodiment, waste active carbon to be processed is conveyed into via the second helical feed screw rod 32 from the second feeding warehouse 31
In second thermal decomposition tube (not shown).The maximum temperature of the second thermal decomposition tube (not shown) of second pyrolysis installation 33 is according to waste active carbon
Ingredient, treating capacity is different and different from, it is preferable that the highest in the second thermal decomposition tube (not shown) of the second pyrolysis installation 33
Temperature is 700 DEG C to 900 DEG C, and residence time of the waste active carbon in the second thermal decomposition tube (not shown) of the second pyrolysis installation is 5
To 30 minutes.The Regenevating Waste Activated Carbon process of the S5 step includes:
A. it drying stage: keeps the second pyrolysis installation 33 in the first predetermined temperature, dries waste active carbon residual moisture and simultaneously produce
Unboiled water steam；In the present embodiment, it is preferable that the first predetermined temperature is 100 DEG C to 300 DEG C.
B. pyrolysis phase: keep the second pyrolysis installation 33 in the second predetermined temperature, the organic matter desorption of waste active carbon absorption
Or decompose, waste active carbon carbonizes to obtain carbon residue；In the present embodiment, it is preferable that the second predetermined temperature is 300 DEG C to 700 DEG C
C. activating and regenerating stage: the vapor for keeping the second pyrolysis installation 33 to generate in third predetermined temperature, desiccation stage
It is reacted with carbon residue, waste active carbon restores charcoal hole and characterization of adsorption, obtains regenerated carbon.In the present embodiment, it is preferable that third is pre-
Determining temperature is 700 DEG C to 900 DEG C.
S6: providing the second separator 34 and carry out isolated desorption gas and regenerated carbon to the second thermal decomposition product,
Desorption gas enters in combustion chamber 26 by the way that connecting tube is (not shown)；
D. UTILIZATION OF VESIDUAL HEAT IN:
S7: waste heat boiler 13 is connected with the first pyrolysis installation 23 and the second pyrolysis installation 33, into the first pyrolysis installation
It is that the second pyrolysis installation 33 provides heat source that 23 high-temperature flue gas, which enters the second pyrolysis installation 33 from the first pyrolysis installation 23, into the
The high-temperature flue gas of two pyrolysis installations 33 enters in 13 furnace of waste heat pot from the second pyrolysis installation 33, and heats the water in waste heat boiler 13
Generating saturated steam is that desiccation apparatus 11 provides heat source.
In S7 step, further comprise the setting of first switch valve 51 the first pyrolysis installation 23 and the second pyrolysis installation 33 it
Between, first switch valve 51 is used to control the on-off between the first pyrolysis installation 23 and the second pyrolysis installation 33, second switch valve 52
It is arranged between the first pyrolysis installation 23 and waste heat boiler 13, second switch valve 52 is for controlling the first pyrolysis installation 23 and waste heat
On-off between boiler 13.
First switch valve 51 is opened, second switch valve 52 is closed, high-temperature flue gas enters the second heat from the first pyrolysis installation 23
Solution device 33 is that the second pyrolysis installation 33 provides heat source, into the high-temperature flue gas of the second pyrolysis installation 33 from the second pyrolysis installation 33
Into in 13 furnace of waste heat pot, and heating the water in waste heat boiler 13 to generate saturated steam is that desiccation apparatus 11 provides heat source.This
When, desiccation apparatus 11, organic dangerous waste pyrolysis system 200, Regenevating Waste Activated Carbon system 300 and waste heat boiler 13 form the money of circulation
Source utilizes system, it is possible to prevente effectively from the waste of resource.
In S7 step, it is further provided third switch valve 53 is arranged between the second pyrolysis installation 33 and waste heat boiler 13,
Third switch valve 53 is for regulating and controlling the on-off between the second pyrolysis installation 33 and waste heat boiler 13.
Third switch valve is opened, first switch valve is opened, closes second switch valve, high-temperature flue gas is from the first pyrolysis installation 23
The second pyrolysis chamber (not shown) into the second pyrolysis installation 33, the first pyrolysis chamber (not shown) mention for the second pyrolysis installation 33
Supplying heat source, into the second pyrolysis chamber (not shown) high-temperature flue gas of the second pyrolysis installation 33 from the second of the second pyrolysis installation 33 the heat
Solution room is (not shown) to be entered in waste heat boiler 13.
First switch valve 51 is closed, second switch valve 52 is opened, closes third switch valve 53, high-temperature flue gas is pyrolyzed from first
The first pyrolysis chamber (not shown) of device 23 is directly entered in waste heat boiler 13, and is heated the water in waste heat boiler 13 and generated saturation
Vapor is that desiccation apparatus 11 provides heat source again, at this point, pyrolysis system of the invention is only handled organic dangerous waste, is given up active
Charcoal regenerative system 300 does not have heat source source, but desiccation apparatus 11, organic dangerous waste pyrolysis system 200 and waste heat boiler 13 are still
Form the utilization of resources system of circulation.
In the present embodiment, it is preferable that the pretreated organic dangerous waste of desiccation enters in first thermal decomposition tube (not shown),
High-temperature flue gas enters in the first pyrolysis chamber (not shown), and high-temperature flue gas does not enter in the first thermal decomposition tube (not shown).Therefore, high temperature
Flue gas (not shown) in the first pyrolysis chamber carries out indirect heating to organic dangerous waste in the first thermal decomposition tube (not shown), can control
The temperature of preparing high-temp flue gas is no more than the fusing point of low-melting compound in organic dangerous waste, avoids in organic dangerous waste pyrolytic process the
One thermal decomposition tube (not shown) interior coking.
In the present embodiment, it is preferable that waste active carbon enters in second thermal decomposition tube (not shown), and high-temperature flue gas enters the
In two pyrolysis chambers (not shown), do not enter in the second thermal decomposition tube (not shown).High-temperature flue gas is to the useless work in the second thermal decomposition tube 332
Property charcoal carry out indirect heating, can control flue-gas temperature no more than waste active carbon absorption low-melting compound fusing point, avoid
Waste active carbon coking in the second thermal decomposition tube 332.
E. gas cleaning:
S8: the exhanst gas outlet of waste heat boiler 13 is connected to dust-extraction unit 14 by gas cleaning step, and high-temperature flue gas is through waste heat
The heat-exchanging tube bundle of boiler 13 is (not shown) cooling, and flue gas after cooling enters dust-extraction unit 14 and is dusted, then through deacidifying device
15 carry out depickling processing, and the flue gas after depickling is discharged through tapping equipment 16.
[embodiment one]
Below in conjunction with to aqueous 60% the dregs of a decoction and aqueous 20% waste active carbon processing to pyrolytic process of the invention
It is further described:
The feedstock property of the above-mentioned dregs of a decoction is analyzed as follows:
Table one: the feedstock property analysis of the dregs of a decoction
The step of carrying out pyrolysis and Regenevating Waste Activated Carbon to the above-mentioned dregs of a decoction using pyrolytic process of the invention is described in detail such as
Under:
Firstly, the dregs of a decoction that above-mentioned water content is 60% are sent to desiccation apparatus by conveying device (not shown)
In 11, and produced from waste heat boiler 13 180 DEG C, the saturated steam dividing wall type contact heat-exchanging of adverse current, water and portion in the dregs of a decoction
Divide volatile organic matter gradually to evaporate to be pulled away, the dehydration dregs of a decoction that remaining moisture content is 18%.In the present embodiment, desiccation apparatus 11
Preferably, using disk granulation drying machine.In other embodiments, desiccation apparatus 11 can also using vacuum belt drier or
Screw dryer.
The pretreated dregs of a decoction of desiccation are transmitted to the first feeding warehouse 21 via conveyer belt (not shown), then via the first spiral shell
Conveying screw rod 22 is revolved out of, the first feeding warehouse 21 is sent into the first pyrolysis installation 23 the first thermal decomposition tube (not shown), and feed rate is
350kg/h, the maximum temperature in the first thermal decomposition tube (not shown) of the first pyrolysis installation 23 are 650 DEG C, using coming from combustion chamber
26 high-temperature flue gas is heated；The dregs of a decoction stop 20 minutes in the first thermal decomposition tube (not shown) of the first pyrolysis installation 23, complete
It is converted into residue and pyrolysis gas entirely, wherein residue flow 83kg/h, pyrolysis gas flow 267kg/h.
Residue and pyrolysis gas are sent into the first separator 24, residue is after cooling water is cooling by the first deslagging spiral
Discharge (not shown), pyrolysis gas enter the burning of combustion chamber 26 and generate high-temperature flue gas, and 26 temperature of combustion chamber controls as 1100 DEG C extremely
1150 DEG C, gas residence time is greater than 2s.
N element average content is 5.06% in the dregs of a decoction used, therefore by the way of being segmented low oxygen combustion, empty by control
Gas excess coefficient and ignition temperature inhibit the generation of nitrogen oxides；Flue gas after burning controls to adjust valve sky (not shown) through temperature
After being cooled to set temperature, into SNCR (selective non-catalytic reduction) denitrification apparatus 27, denitrfying agent uses 10% urea liquid, most
Whole flue gas emission amount of nitrogen oxides is 320mg/Nm3, meets national regulation limit value.
The first pyrolysis chamber that flue gas after denitration enters the first pyrolysis installation 23 is (not shown) for the confession of dregs of a decoction pyrolytic reaction
Heat, wherein heat supply temperature is 750 DEG C, and the flue gas after heating the first pyrolysis installation 23 enters the second of regenerating active carbon system 300
The second pyrolysis chamber (not shown) of pyrolysis installation 33.
Aqueous 20% waste active carbon is sent into the second pyrolysis from the second feeding warehouse 31 through the second helical feed screw rod 32 to fill
It sets in 33 the second thermal decomposition tube (not shown), treating capacity 200kg/h, waste active carbon enters the second heat of the second pyrolysis installation 33
The wall surface heat exchange that solution pipe (not shown) is gradually heated with high-temperature flue gas heats up, experience is dry, adsorbate is desorbed, adsorbate carbonizes,
Adsorbate gasification realizes active carbon hot recycling.The desorption gas of generation is transported to burning, regenerated carbon in combustion chamber 26
After the second separator 24, it is discharged into after water cooled in regenerated carbon collection device 36.
The flue gas that waste active carbon thermal regeneration system 300 comes out recycles heat from the second pyrolysis installation 33 into waste heat boiler 13
Amount, flue gas are down to 200 DEG C by the heat-exchanging tube bundle (not shown) of waste heat boiler 13 and generate 180 DEG C of saturated steams, saturated water
Steam enters desiccation apparatus 11 and continues as the offer heat source of desiccation apparatus 11；
Flue gas after cooling enters bag filter 14, removes the particulate matter in flue gas, then through 15 depickling of deacidifying device at
Reason, wherein for deacidifying device 15 using 15% lime stone slurry, tail gas is detected qualified qualified discharge, tails assay result column
In subordinate list two.
| Project | Nitrogen oxides | Sulfur dioxide | CO | Dioxin |
| Limit value mg/m3 | 500 | 300 | 80 | 0.5TEQng/m3 |
| Measured value mg/m3 | 320 | 21 | 17 | 0.03TEQng/m3 |
Table two: the detection parameters of 1 emission of embodiment
[embodiment two]
One step S2 Chinese medicine slag feed rate of embodiment is changed to 600kg/h, controlling temperature in the first pyrolysis installation 23 is
850 DEG C, wherein pyrolysis gas 509kg/h is obtained, solid residue 91kg/h.Correspondingly, waste active carbon inlet amount is changed in step S6
300kg/h, temperature control in the second thermal decomposition tube (not shown) of the second pyrolysis installation 33 is at 800 DEG C or so, heat of the invention
Solution technique still is able to that stabilization is maintained voluntarily to operate, and by-product 0.3t/h saturated steam (184 DEG C) external application, and tail gas is closed through detection
Lattice qualified discharge, tail gas inspection results are listed in table three.
| Project | Nitrogen oxides | Sulfur dioxide | CO | Dioxin |
| Limit value mg/m3 | 500 | 300 | 80 | 0.5TEQng/m3 |
| Two measured value mg/m of embodiment3 | 410 | 40 | 19 | 0.05TEQng/m3 |
Table three: the detection parameters of 2 emission of embodiment
The rest part of embodiment two is the same as example 1, and is repeated no more.
Although the present invention is disclosed as above with preferred embodiment, however, it is not intended to limit the invention, any to be familiar with ability
The technical staff in domain, without deviating from the scope of the technical scheme of the present invention, all using the technology contents pair of the disclosure above
Technical solution of the present invention makes many possible changes and modifications or equivalent example modified to equivalent change.Therefore, all
Without departing from the content of technical solution of the present invention, according to the present invention technical spirit any simple modification made to the above embodiment,
Equivalent variations and modification, all shall fall within the protection scope of the technical scheme of the invention.
Claims (10)
1. a kind of pyrolytic process handles organic dangerous waste and waste active carbon, which comprises the following steps:
S1: desiccation apparatus is provided, desiccation pretreatment is carried out to organic dangerous waste to be processed；
S2: the pretreated organic dangerous waste of desiccation is sent into the first pyrolysis installation and carries out pyrolysis processing, pyrolysis obtains the first pyrolysis
Product；
S3: the first separator is provided, the first thermal decomposition product is separated, respectively obtain pyrolysis gas and residue；
S4: combustion chamber is provided, combustion chamber is connected with the first separator, pyrolysis gas enters burning from the first separator
Room, pyrolysis gas burn in the combustion chamber and generate high-temperature flue gas, and it is that high-temperature flue gas, which enters the first pyrolysis installation from combustion chamber,
One pyrolysis installation provides heat source；
S5: waste active carbon to be processed is sent into the second pyrolysis installation, the second pyrolysis installation carries out pyrolysis processing to waste active carbon
Generate the second thermal decomposition product；
S6: the second separator is provided, isolated desorption gas and regenerated carbon is carried out to the second thermal decomposition product, gas is desorbed
Body enters in combustion chamber；
S7: waste heat boiler is connected with the first pyrolysis installation and the second pyrolysis installation, into the high-temperature flue gas of the first pyrolysis installation
Enter the second pyrolysis installation from the first pyrolysis installation and provide heat source for the second pyrolysis installation, into the high temperature cigarette of the second pyrolysis installation
Gas enters in waste heat boiler from the second pyrolysis installation, and heats the generation saturated steam of the water in waste heat boiler and mention for desiccation apparatus
Supplying heat source.
2. pyrolytic process according to claim 1, it is characterised in that: in step S7, in the first pyrolysis installation and the second heat
It solves and first switch valve is set between device, first switch valve is used to control logical between the first pyrolysis installation and the second pyrolysis installation
It is disconnected, second switch valve is set between the first pyrolysis installation and waste heat boiler, and second switch valve is for controlling the first pyrolysis installation
On-off between waste heat boiler opens first switch valve, closes second switch valve, and high-temperature flue gas enters from the first pyrolysis installation
Second pyrolysis installation provides heat source for the second pyrolysis installation.
3. pyrolytic process according to claim 2, it is characterised in that: in step S7, it is further provided third switch valve is set
It sets between the second pyrolysis installation and waste heat boiler, third switch valve is for regulating and controlling between the second pyrolysis installation and waste heat boiler
On-off.
4. pyrolytic process according to claim 3, it is characterised in that: open third switch valve, open first switch valve, close
Second switch valve is closed, high-temperature flue gas enters the second pyrolysis installation from the first pyrolysis installation and provides heat source for the second pyrolysis installation, into
The high-temperature flue gas for entering the second pyrolysis installation enters in waste heat boiler from the second pyrolysis installation.
5. pyrolytic process according to claim 3, it is characterised in that: close third switch valve, close first switch valve, open
Second switch valve is opened, high-temperature flue gas is directly entered in waste heat boiler from the first pyrolysis installation.
6. pyrolytic process according to claim 1, it is characterised in that: the first pyrolysis installation includes the first pyrolysis chamber and is located at
First indoor first thermal decomposition tube of pyrolysis, organic dangerous waste enter in first thermal decomposition tube, and high-temperature flue gas enters the first heat
Solution is indoor, does not enter in the first thermal decomposition tube, and high-temperature flue gas carries out indirect heating to organic dangerous waste in the first thermal decomposition tube.
7. pyrolytic process according to claim 1, it is characterised in that: the second pyrolysis installation includes the second pyrolysis chamber and is located at
Second indoor second thermal decomposition tube of pyrolysis, the waste active carbon enter in second thermal decomposition tube, and high-temperature flue gas enters the second heat
Solution is indoor, and high-temperature flue gas does not enter in the second thermal decomposition tube, and high-temperature flue gas add indirectly to the waste active carbon in the second thermal decomposition tube
Heat.
8. pyrolytic process according to claim 7, it is characterised in that: further comprise the first feeding warehouse and the first spiral transferring
Screw rod is sent, it further comprises the second charging that the first helical feed screw rod, which is set between the first feeding warehouse and the first pyrolysis installation,
Storehouse and the second helical feed screw rod, the second helical feed screw rod is set between the second feeding warehouse and the second pyrolysis installation, organic
Dangerous waste is conveyed into the first thermal decomposition tube via the first helical feed screw rod from the first feeding warehouse, and waste active carbon is via the second spiral transferring
Screw rod is sent to be conveyed into the second thermal decomposition tube from the second feeding warehouse.
9. pyrolytic process according to claim 1, it is characterised in that: further provide for auxiliary burner and be arranged in combustion chamber
Input end, auxiliary burner sprays into combustion gas into combustion chamber by temperature control feedback to adjust the indoor temperature of burning.
10. pyrolytic process according to claim 1, it is characterised in that: gas cleaning step S8 is further provided for, by waste heat
The exhanst gas outlet of boiler is connected to dust-extraction unit, and heat-exchanging tube bundle of the high-temperature flue gas through waste heat boiler is cooling, flue gas after cooling into
Enter dust-extraction unit to be dusted, then carry out depickling processing through deacidifying device, the flue gas after depickling is discharged through tapping equipment.
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| CN111550792A (en) * | 2020-03-26 | 2020-08-18 | 安徽紫荆花壁纸股份有限公司 | A system and method for comprehensive utilization of waste treatment for wallpaper processing |
| CN113028426A (en) * | 2021-02-22 | 2021-06-25 | 中国汽车工业工程有限公司 | Harmless decrement process and heat energy recycling method of paint waste residues |
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| CN104772114A (en) * | 2015-03-13 | 2015-07-15 | 无锡中天固废处置有限公司 | Organic adsorption saturated active carbon regeneration device |
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