CN106082576A - A kind of low temperature continuous pyrolysis processes mud fixed bed reactors and method - Google Patents
A kind of low temperature continuous pyrolysis processes mud fixed bed reactors and method Download PDFInfo
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- CN106082576A CN106082576A CN201610654687.XA CN201610654687A CN106082576A CN 106082576 A CN106082576 A CN 106082576A CN 201610654687 A CN201610654687 A CN 201610654687A CN 106082576 A CN106082576 A CN 106082576A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/10—Treatment of sludge; Devices therefor by pyrolysis
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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
- C10B31/00—Charging devices
- C10B31/06—Charging devices for charging horizontally
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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
- C10B33/00—Discharging devices; Coke guides
- C10B33/02—Extracting coke with built-in devices, e.g. gears, screws
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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
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/02—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with stationary charge
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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
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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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/40—Valorisation of by-products of wastewater, sewage or sludge processing
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- General Chemical & Material Sciences (AREA)
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- Treatment Of Sludge (AREA)
Abstract
The present invention relates to a kind of low temperature continuous heat fixed bed reactors and method.Reactor reaction utensil of the present invention has sludge inlet, housing, reative cell, solid discharge, sludge inlet is positioned on solid discharge, reative cell has flitch, cloth spiral, discharging spiral, feed auger, flitch includes feed end and discharge end, cloth spiral is under sludge inlet, feed end top, discharging spiral is on discharge end top, and discharge end is on solid discharge；Cloth spiral includes center bolt and left and right helical blade, and center bolt crosses left and right helical blade, and left and right helical blade is perpendicular to the centrage of center bolt and becomes axial symmetry, 1/3～1/2 that distance is sludge inlet bore；Feed auger is fixed on the interlude of cloth spiral vertical with cloth spiral.The present invention can realize continuous feeding and discharging under the conditions of hot, it is not necessary to mud is carried out pretreatment, and equipment failure rate is low, high financial profit.
Description
Technical field
The present invention relates to field of sludge treatment, particularly relate to a kind of low temperature continuous pyrolysis and process the fixed bed reaction of mud
Device, and the method utilizing described reactor for treatment mud.
Background technology
Domestic sludge can produce solid-state, liquid and gaseous products through Overheating Treatment, and these products are made into recyclable, Yi Li
With, easily transport and the energy form that easily stores, can heat supply generating or be used as chemical industry and the raw material of other industries.Above-mentioned heat treatment work
Skill includes carbonization, gasifies, is pyrolyzed, liquefies or other related process.
Wherein, being pyrolyzed the one as Technology for Heating Processing, the reactor used has multiple, commonly uses including commercial production
Moving bed, fixed bed, rotary kiln, fluid bed, also include ablation bed and shower furnace etc., is mainly used in reclaiming certain in thermal decomposition product
One or both materials.
Moving bed pyrolysis technique belongs to slow pyrolysis process, and the secondary response rate of intermediate product is low, and pyrolysis oil productivity is high.But
Being the external-heat heat-supplying mode used, heat transfer efficiency is relatively low, causes whole system not operate at full capacity；Fluidized bed pyrolysis technique
Belonging to fast pyrolysis process, the rate of heat addition is fast, the gas phase time of staying is short, and efficiency of utilization is high, it is possible to decrease the generation of secondary response,
Pyrolysis oil productivity is higher.But material pyrolytic process is in sulphided state, causes dustiness in pyrolytic behavior high, it is more difficult to process；Burn
Erosion bed pyrolytic process is by reaction mass and scorching hot metal surface direct contact heat transfer, makes material be brought rapidly up and cracks.Should
Technique pyrolysis time is short, and response speed is fast, and oil yield is high, but cannot realize the seriality of material pyrolysis, can only carry out batch
Batch (-type) is pyrolyzed；Rotary kiln pyrogenation technique is suitable for almost any solid waste material, and the aqueous higher material of oil-containing, such as dirt
The thickness class material such as mud, greasy filth, then cannot directly use which to be pyrolyzed；Conventional fixed-bed pyrolysis system is batch feed, no
Can run the most continuously, and pyrolytical condition is difficult to keep for a long time.
For the problems referred to above, prior art CN104030535A discloses a kind of mud interior-heat continuous shale oven pyrolysis material
Method.Send into low temperature continuous shale oven after the pretreatment such as raw sludge drying, pelletize, use screw feeder conveying material,
Transmit material by conveying plate chain, reverberatory furnace provide heat.The Toxic heat that whole process can will remain in raw sludge
Being decomposed into nontoxic intermediate, heavy metal is cured, is passivated, and superbacteria, virus, through thorough harmless treatment, and can obtain
To the material such as combustion gas, biomass, reach the purpose turned waste into wealth.The method, be through certain when processing thickness class material
Preprocessing process, and skewness on conveying plate chain, impact pyrolysis effect, for the mud that oil content is higher, pyrolysis plasticizing
If residue after sticks to affect on transfer plate chain discharging, even needs to stop.
Prior art CN102559222A discloses the method for a kind of low temperature distillation stove pyrolysis material.This method for pyrolysis uses
Horizontal gas retort, before pyrolysis starts each time, first needs to stop unloading reaction after reactor heat supply, question response device cooling down
Device fire door or bell, the solid product of a collection of pyrolysis residual before taking out, needs are artificial adds next batch heat in reactor
The material solved.Therefore the method cannot realize material hot under the conditions of continuous feeding and discharging, without automatic distributing and discharging functions, real
Existing high temperature pyrolysis fixed gas is from for providing heat.Input and output material process need to rise gentleness cooling to reactor, reduces the place of device
Reason ability and efficiency, add fault rate.
Summary of the invention
In view of the deficiencies in the prior art, it is desirable to provide a kind of novel low temperature continuous pyrolysis processes the fixing of mud
Bed reactor, and the method utilizing this reactor for treatment mud.This reactor is stable, easily operates, and can enter mud
Row batch heat treatment, again can continuous feed and discharging under the conditions of hot.
The present invention proposes a kind of low temperature continuous pyrolysis and processes mud fixed bed reactors, and described reactor has mud and enters
Mouth, housing, reative cell, solid discharge, the horizontal level of described sludge inlet sets high than the horizontal position of described solid discharge；
Described reative cell has flitch, cloth spiral, discharging spiral, feed auger；
Described flitch includes feed end and discharge end, and described cloth spiral is arranged under described sludge inlet, is positioned at institute
State feed end top；Described discharging spiral is arranged on described discharge end top, and described discharge end is positioned on described solid discharge；
Described cloth spiral includes center bolt, left-hand screw blade, right-hand screw blade；Described center bolt crosses a described left side
Helical blade and right-hand screw blade, the centrage that described left-hand screw blade is perpendicular to described center bolt with right-hand screw blade becomes axle
Symmetry, distance between the two is the 1/3～1/2 of described sludge inlet bore；
Described feed auger is fixed on the interlude of described cloth spiral vertical with described cloth spiral.
Further, the lower limb of described left-hand screw blade and right-hand screw blade and the vertical dimension of described flitch be 50～
150, preferably 80；Described left-hand screw impeller clearance and right-hand screw impeller clearance are placed equidistant or displacement is arranged.
Further, feed end and the discharge end of described flitch are provided with drive bearing, are used for driving described flitch continuous
Rotate；Described drive bearing has two or more.
Further, described housing includes reactor wall, support platform, support；
Described reactor wall includes furnace roof, sidewall, furnace bottom, is used for sealing described reative cell；
Described support platform is arranged under described flitch；
Described support is fixed in described support platform, is used for connecting described drive bearing.
Further, described reative cell includes radial canal and oil gas vent；
Described radial canal is heat accumulation type radiant tube, is arranged on the top of described flitch and parallel with described flitch；
Vertical dimension between described radial canal and described flitch is 100～300mm, preferably 150；
Described oil gas vent is arranged on described sidewall of reactor, and is positioned at the bottom of described radial canal.
Further, above-mentioned reactor also includes feeding warehouse, push-pull valve, solid collecting bin；
Described feeding warehouse is arranged on described feed auger top, and described push-pull valve is arranged on described feeding warehouse bottom；
Described solid collecting bin connects the discharge end of described flitch；
It is provided with level-sensing device between described push-pull valve and described cloth spiral；
Described feeding warehouse and described solid collecting bin have one or more.
The invention allows for a kind of method utilizing above-mentioned reactor for treatment mud, said method comprising the steps of:
Mud is transported to by described sludge inlet the interlude of described cloth spiral；
Described mud is distributed uniformly along the flitch both sides of described continuous rotation, after unlatching discharging spiral transports reaction simultaneously
Solid residue, it is ensured that charging and the seriality of discharging.
Further, described step also includes: the pyrolysis oil air cooling that described oil gas vent is discharged obtains pyrolysis oil and heat
Vent one's spleen.
In said method, described moisture percentage in sewage sludge≤95wt%, its height on described flitch is 150～300.
In said method, in described reative cell, temperature is 350～1200 DEG C, and pressure is-2～5kPa.
The present invention, by using unique cloth spiral structure, can realize mud uniform distribution on flitch.On flitch
Side has been evenly arranged many radial canals, and raw material is static relative to flitch and radial canal in pyrolytic process, it is ensured that it is uniformly subject to
Heat.
During pyrolysis processing, by flitch, feed auger, cloth spiral, the joint operation of discharging spiral, can be not
Under conditions of blowing out, it is achieved the continuous feed of reactor and discharging.The high-temperature hot that pyrolytic reaction produces is vented one's spleen and be may be recovered profit
With, reduce heat loss, improve Treatment of Sludge and receive energy efficiency and the economic benefit of process, therefore there is bigger development excellent
Gesture and application prospect.
Accompanying drawing explanation
Fig. 1 is the left view that low temperature continuous pyrolysis processes mud fixed bed reactors.
Fig. 2 is the top view that low temperature continuous pyrolysis processes mud fixed bed reactors.
Fig. 3 is the front view that low temperature continuous pyrolysis processes mud fixed bed reactors.
Reference in accompanying drawing is as follows:
1-housing；
2,2a, 2b, 2c-radial canal；
3-center bolt；3a-discharging spiral；3b-cloth spiral；
4-flitch；
5-feeding warehouse；5a-sludge inlet；
6-push-pull valve；
7-support；
8-reative cell；
9-drive bearing；
10-substrate；
11-support platform；
12-oil gas vent；
13-feed auger；
14-solid collecting bin；14a-solid discharge.
Detailed description of the invention
Below in conjunction with drawings and Examples, the detailed description of the invention of the present invention is described in more details, in order to energy
The advantage being enough more fully understood that the solution of the present invention and various aspects thereof.But, specific embodiments described below and enforcement
Example is only descriptive purpose rather than limitation of the present invention.
These fixed bed reactors can be not only used for resource and recycle organic compound, can be used for again harmless treatment and discard
Thing, including four parts: feed system, response system, discharge system, housing.Show respectively below in conjunction with Fig. 1, Fig. 2, Fig. 3
The left view of fixed bed reactors, top view, front view, illustrate the structure between these four parts and relation thereof.
1. housing: as shown in Figure 1, the housing 1 of fixed bed reactors includes reactor wall, support 7, substrate 10, supports and put down
Platform 11.
Reactor wall includes furnace roof, sidewall, furnace bottom, is used for sealing whole reative cell 8 so that the reaction gas in reative cell 8
Atmosphere is sufficiently spaced from ambient atmosphere.
2. feed system: as shown in Figure 1, feed system includes feeding warehouse 5, push-pull valve 6, sludge inlet the most successively
5a.The quantity of feeding warehouse 5 can be one or more.
3. discharge system: as shown in Figure 1, discharge system is made up of solid discharge 14a and solid collecting bin 14, solid discharge
14a is under sludge inlet 5a, and is both provided with feeding chute, for charging and the discharging of reactor.Solid collecting bin 14
Quantity can be one or more.
4. response system: response system includes reative cell 8, for the pyrolysis of mud.
As shown in Figure 3, the bottom of reative cell 8 is provided with flitch 4, is positioned on support platform 11.For the ease of describing,
The two ends of flitch 4 are respectively designated as feed end and discharge end.By Fig. 1, discharge end is by solid discharge 14a and solid collecting bin
14 connect.It is respectively provided with a drive bearing 9 at feed end and discharge end.One end of support 7 is fixed in support platform 11, separately
One end connects drive bearing 9.
In drive bearing 9, one is drivewheel, and one is driven pulley, for driving the continuous rotation of flitch 4.According to need
Wanting, can arrange several driven pulleys at the interlude of flitch 4, driven pulley upper end contacts with flitch 4 and plays a supporting role, and lower end is solid
It is scheduled in support platform 11.
As shown in Figure 1, cloth spiral 3b be positioned under sludge inlet 5a, the top of flitch 4 feed end；Discharging spiral 3a position
In the top of flitch 4 discharge end, and discharge end is positioned on solid discharge 14a.Arrange between cloth spiral 3b and push-pull valve 6
There is level-sensing device.
Shown in Fig. 2 and Fig. 3, cloth spiral 3b and discharging spiral 3a is formed by helical blade and center bolt 3, center
Screw rod 3 crosses helical blade.In the embodiment of the present invention, the gap between helical blade is placed equidistant, its lower limb and flitch 4
Distance is 50～150, and wherein preferred distance is 80.
In other embodiments, the gap between helical blade can use the mode that displacement is arranged, and near mid portion
Helical blade gap, helical blade gap-ratio center bolt two ends is little so that mud distribution on flitch 4 is more uniform.
Shown in Fig. 2 and Fig. 3, feed auger 13 is fixed on the mid portion of cloth spiral 3b, and with cloth spiral
3b is vertical.In Fig. 2, the helical blade of cloth spiral 3b includes left-hand screw blade and right-hand screw blade.Center bolt 3 crosses left spiral shell
Vane and right-hand screw blade.The centrage that left-hand screw blade is perpendicular to center bolt 3 with right-hand screw blade becomes axial symmetry.The present invention
In embodiment, the spacing of left-hand screw blade and right-hand screw blade is the 1/3～1/2 of sludge inlet 5a bore.
In the embodiment of the present invention, the special tectonic of cloth spiral 3b so that mud from the mid portion of cloth spiral 3b to
Two end motions, it is possible to reduce mud is with in the operating distance of cloth spiral 3b, and the wider flitch 4 of realization uniform point of material
Cloth, preferred implementation is for using single cloth spiral.
In other embodiments, deflector can be set up at the feeding chute of sludge inlet 5a, contribute to the uniform of mud
Distribution.
As shown in Figure 2, reative cell 8 is provided with 3 radial canals, respectively 2a, 2b, 2c, is denoted as in Fig. 1 and Fig. 3
Radial canal 2.In other embodiments, the quantity of radial canal 2 can be any amount in addition to 3.In the embodiment of the present invention
In, radial canal 2 is evenly arranged in reative cell 8, and parallel with flitch 4.Radial canal 2 and the spacing of the mud of layout on flitch 4
The least, the vertical height of its distance flitch 4 is 100～300, preferably 150.
As shown in Figure 1, being provided with 2 oil gas vents 12, be positioned under radial canal 2 in reative cell 8 on sidewall, its position is straight
Connect and affect flow direction and the time of staying being pyrolyzed oil gas in reative cell 8.In other embodiments, oil gas vent 12 can be except 2
Other any amount beyond individual.
The embodiment of the present invention preferred square reactor, it is possible to be designed as cylindrical reactor or other shapes of reaction
Device.The structure of employing square reactor is advantageously in the setting of radial canal 2, so that mud is heated evenly, it is ensured that pyrolysis
Uniformly producing and flowing of oil gas.
The process flow process of the embodiment of the present invention is as follows:
1. ingredient requirement
The fixed bed reactors of the embodiment of the present invention to raw material without be strict with, it is adaptable to process moisture content be less than
The mud of 95wt% (wt% is mass percent), such as oil field oiliness mud, containing mine dust mud, domestic sludge, industrial sludge etc..
2. charging and cloth process
In the case of push-pull valve 6 cuts out, in feeding warehouse 5, add mud.Stirring rod can be set in feeding warehouse 5, use
In the fluffy material phenomenon preventing material.Mud is firstly stored in feeding warehouse 5, opens push-pull valve 6, mud under gravity, from
The feeding chute that sludge inlet 5a lower end is arranged is slipped to downwards the front end of feed auger 13 in reative cell 8.In feed auger
Under the effect of 13, mud is continuously conveyed the mid portion to cloth spiral 3b.While cloth spiral 3b operates, flitch 4
Accept mud and drive it to be fed forward, making whole fixed bed reactors be covered with mud uniformly.Wherein, feed auger 13 also rises
To sealing function, isolation reative cell 8 and sludge inlet 5a, meet the needs of anoxybiotic in reative cell 8.
Level-sensing device can be used for detection and enters the mud height of reative cell 8, by regulation feed auger 13 and cloth spiral 3b,
The inlet amount and the cloth doses that make mud match.
Noble gas access port can be set at push-pull valve 6, open push-pull valve 6 feed in reactor time, mud can
It is sent to feed auger under the assistance of the air-flow of noble gas formation.This noble gas may select nitrogen, or is other non-oxygen
The property changed gas, meets the anoxybiotic requirement of pyrolytic reaction in reative cell 8.
Fixed bed reactors of the present invention can use the mode that single feeds, it is possible to uses the mode of continuous feed.When required
When the sludge quantity of process is less, the fixed bed reactors in the embodiment of the present invention can be used to operate.If the mud processed
Amount is relatively big, can increase the area of flitch 4, keeps the continuous rotation of flitch 4, make material on flitch 4 during pyrolytic reaction
Pyrolytic reaction is completed, it is ensured that charging and the seriality of discharging from feed end to discharge end.
3. entry level
In the pyrolytic process of mud, in order to ensure the seriality of pyrolytic reaction, by the single sewage sludge storage of feeding warehouse 5
Amount cannot be less than the single mud cloth doses of flitch 4.During pyrolytic reaction, feeding warehouse 5 stores a certain amount of mud,
The mud height ensured in reative cell 8 on flitch 4 is 150～300.
4. pyrolytic reaction condition
The pyrolytic reaction occurred in these fixed bed reactors is carried out in the range of 350～1200 DEG C.Mud is by dirt
After mud entrance 5a enters reative cell 8, progressively heat up under the effect of radial canal 2.First it is dried, the water in removing mud
Point, devolatilization the most again, form pyrolysis oil gas product and hot solid residue product through pyrolytic reaction.
Possibly together with the organic components of a certain amount of not heated volatilization in solid residue product, by it is carried out work
Industry is analyzed, and can record the volatile matter content in solid residue less than 10wt% (wt% is weight percentage).
During pyrolytic reaction, reative cell 8 to be controlled is in anoxybiotic atmosphere, and maintains pressure in the range of-2～5kPa.
5. mode of heating
The mode of heating of these fixed bed reactors may select Electric heating, fuel mode of heating, high-temperature plasma add
Hot mode etc., the embodiment of the present invention preferred heat accumulation type radiant tube mode of heating, meet combustion heating system and material heat in device
The isolation of solution system.
The heating rate of radial canal 2 controls at 20～60 DEG C/min, and the different temperature rise periods select different heating rates.When
When mud temperature is less than 280 DEG C, the heating rate of radial canal 2 controls at 40～60 DEG C/min, when mud temperature is 280～450
DEG C time, the heating rate of radial canal 2 controls at 20～40 DEG C/min, when mud temperature is more than 450 DEG C, the intensification of radial canal 2
Rate controlled is at 20～60 DEG C/min.
6. discharging process and the collection of solid residue
, start discharging spiral 3a, discharging spiral 3a and make solid while cloth starting cloth spiral 3b in flitch 4
Bottoms product by the discharge end of flitch 4 to the unidirectional output of solid collecting bin 14.So can meet same at uniform distribution of flitch 4
Time, last reacted solid residue is carried out discharging, thus ensures charging and the seriality of discharging in reactor.
When the fixed bed reactors of the embodiment of the present invention are used as harmless treatment garbage device, by discharging spiral 3a
The hot solid residue product discharged is powder, and it directly can be blended in feed product as solid thermal carriers, is used for drying
Dry raw material.Screening separation can be carried out by screening plant through drying the dilution mixing material of cooling, obtain solid product.This screening
Device can be directly mounted at the top of feeding warehouse 5, it is possible to the most independent placement.
7. the recycling of oil gas it is pyrolyzed
The pyrolysis oil gas produced in the embodiment of the present invention is quickly discharged by oil gas vent 12, uses chilling method by discharge
Pyrolysis oil gas quickly cools down, and obtains more pyrolysis oil.And the pyrolysis oil gas time of staying in reative cell 8 should be shortened, it is to avoid
The second pyrolysis of pyrolysis oil gas, improves the productivity of pyrolysis oil.The pyrolysis gas obtained can directly be drawn by conveyance conduit as thermal source
Entering in the burner of heat accumulation type radiant tube, the thermal source as radial canal burns for it, it is provided that the heat needed for reaction.
During pyrolytic reaction, the top layer mud on flitch 4 is first pyrolyzed, and is pyrolyzed after lower floor's mud.Lower floor's pyrolyzing sludge
The carbon residue that the pyrolysis oil gas produced produces after first passing through the pyrolyzing sludge reaction on its upper strata, i.e. lower floor can be worn by the carbon residue on upper strata
The pyrolysis oil gas crossed plays the effect of filtration.
By filtration, the carbon granule in lower floor's pyrolysis oil gas and pollutant can be removed.This filtration is by many factors
Impact, including pyrolysis oil gas in carbon granule and the particle diameter of pollutant, the height of mud on flitch 4, pyrolysis oil gas flow velocity etc..
According to different process requirements, may select and set up catalyst layer in reative cell 8, be used for regulating in gas different group
The content divided.
The fixed bed reactors of the embodiment of the present invention can be used as resource and recycle organic compound device, former extracting
Oily timesharing in material, can discharge back segment at pyrolysis gas and set up gas purge system, for improving the quality of pyrolysis gas.
In the embodiment of the present invention, fixed bed reactors discharging required time after being fed to pyrolyzing sludge is 1.5～5h, should
Time can be affected by the physical property of mud, single inlet amount, heating rate etc..
The fixed bed reactors of the embodiment of the present invention are with one of them difference of conventional fixed bed reactor: the present invention
In fixed bed reactors after the mud having processed single batch, reactor, without lowering the temperature, just can carry out next group mud
Cloth and the discharging of last consignment of solid residue.Therefore, the radial canal 2 in reactor of the present invention only need to be carried out when feeding first
Go into operation igniting, in ensuing whole continuous running, maintains the normal heating temperature of radial canal 2.Thus, instead
Answer in device running, it is to avoid because the liter gentleness of reactor is lowered the temperature by charging each time and discharging, reduce equipment failure rate；
The two of difference are: the fixed bed reactors of the present invention can be by controlling between cloth spiral 3b, flitch 4, discharging spiral 3a
Exploitation speed, it is achieved continuous print charging and discharging in pyrolytic process.
Embodiment
The industrial greasy filth provided by CNOOC is as feed product, and material is sent directly in feeding warehouse 5, opens push-pull valve 6,
The material downward landing of feeding chute at sludge inlet 5a under gravity, enters into the front end of feed auger 13, is entering
Under the transport of material spiral 13, the mid portion of cloth spiral 3b delivered to by material, carries with drive bearing 9 under cloth spiral 3b rotates
Dynamic lower material, by uniform distribution, moves horizontally to discharge end simultaneously, controls cloth spiral 3b and the exploitation speed of flitch, make whole
Reactor fabric thickness is 200mm, after whole reative cell 8 cloth completes, closes push-pull valve 6.
Open radial canal combustion system, when temperature of charge less than 280 DEG C time, control radial canal 2 heating rate 40 DEG C/
Min, when temperature of charge is higher than 280 DEG C, control radial canal 2 heating rate is at 25 DEG C/min, and the pyrolysis oil gas of generation is by oil gas
Outlet 12 entrance condenser system, reclaims pyrolysis oil.Uncooled pyrolysis gas is introduced directly in radial canal 2 as fuel combustion.Whole
Individual pyrolytic process Stress control is within 500Pa.After pyrolytic process does not the most produce pyrolysis oil gas, carry out the second batch oil
The charging of mud, while charging, reacted carbon residue last to fixed bed reactors carries out discharging, it is ensured that input and output material continuous
Property.The carbon residue transferred out is sent in solid collecting bin 14 and is stored.
Process described in the embodiment of the present invention can long-term smooth operation, the product of obtained more stable thermal decomposition product
Rate is shown in Table 2.
Table 1 CNOOC industrial greasy filth analysis result
Table 2 thermal decomposition product analytical data (after water)
| Project | Pyrolysis oil | Pyrolysis gas | Solid residue |
| Productivity (%) | 64.63 | 24.33 | 14.85 |
(remarks: MadRepresent air-dried moisture, AadRepresent empty dry basis ash content, VadRepresent empty butt volatile matter, FCadRepresent sky
Butt fixed carbon, St,adRepresent empty butt sulfur, CadRepresent empty butt carbon, HadRepresent empty butt hydrogen, Qb.arUnit be MJ/
Kg, % are mass percent.)
Process of the present invention can long-term smooth operation, equipment failure rate is extremely low.
It should be noted that each embodiment above by reference to described by accompanying drawing is only in order to illustrate rather than restriction originally
The scope of invention, it will be understood by those within the art that, the most right
Amendment that the present invention is carried out or equivalent, all should contain within the scope of the present invention.Additionally, indication unless the context
Outward, the word occurred in the singular includes plural form, and vice versa.It addition, unless stated otherwise, then any embodiment
All or part of can use in conjunction with all or part of of any other embodiments.
Claims (10)
1. low temperature continuous pyrolysis processes mud fixed bed reactors, and described reactor has sludge inlet, housing, reaction
Room, solid discharge, the horizontal level of described sludge inlet sets high than the horizontal position of described solid discharge；
Described reative cell has flitch, cloth spiral, discharging spiral, feed auger；
Described flitch includes that feed end and discharge end, described cloth spiral are arranged under described sludge inlet, be positioned at described in enter
Material end top；Described discharging spiral is arranged on described discharge end top, and described discharge end is positioned on described solid discharge；
Described cloth spiral includes center bolt, left-hand screw blade, right-hand screw blade；Described center bolt crosses described left-hand screw
Blade and right-hand screw blade, the centrage that described left-hand screw blade is perpendicular to described center bolt with right-hand screw blade becomes axle pair
Claiming, distance between the two is the 1/3～1/2 of described sludge inlet bore；
Described feed auger is fixed on the interlude of described cloth spiral vertical with described cloth spiral.
Reactor the most according to claim 1, it is characterised in that described left-hand screw blade and the lower limb of right-hand screw blade
It is 50～150 with the vertical dimension of described flitch, preferably 80；Described left-hand screw impeller clearance and right-hand screw impeller clearance
It is placed equidistant or displacement is arranged.
Reactor the most according to claim 1, it is characterised in that feed end and the discharge end of described flitch are provided with transmission
Bearing, is used for driving described flitch to rotate continuously；The quantity of described drive bearing is two or more.
Reactor the most according to claim 3, it is characterised in that described housing includes reactor wall, support platform, props up
Frame；
Described reactor wall includes furnace roof, sidewall, furnace bottom, is used for sealing described reative cell；
Described support platform is arranged under described flitch；
Described support is fixed in described support platform, is used for connecting described drive bearing.
Reactor the most according to claim 4, it is characterised in that described reative cell includes radial canal and oil gas vent；
Described radial canal is heat accumulation type radiant tube, is arranged on the top of described flitch and parallel with described flitch；
Vertical dimension between described radial canal and described flitch is 100～300mm, preferably 150；
Described oil gas vent is arranged on described sidewall of reactor, is positioned at the bottom of described radial canal.
Reactor the most according to claim 1, it is characterised in that also include feeding warehouse, push-pull valve, solid collecting bin；
Described feeding warehouse is arranged on described feed auger top, and described push-pull valve is arranged on described feeding warehouse bottom；
Described solid collecting bin connects the discharge end of described flitch；
It is provided with level-sensing device between described push-pull valve and described cloth spiral；
Described feeding warehouse and described solid collecting bin have one or more.
7., by a method for the reactor for treatment mud one of claim 1-6 Suo Shu, said method comprising the steps of:
Mud is transported to by described sludge inlet the interlude of described cloth spiral；
Described mud is distributed uniformly along the flitch both sides of described continuous rotation, opens discharging spiral simultaneously and transports solid after reaction
Residue, it is ensured that charging and the seriality of discharging.
Method the most according to claim 7, it is characterised in that described step also includes: the heat that described oil gas vent is discharged
Solve oil gas cooling and obtain pyrolysis oil and pyrolysis gas.
Method the most according to claim 7, it is characterised in that described moisture percentage in sewage sludge≤95wt%, it is at described flitch
On height be 150～300.
Method the most according to claim 7, it is characterised in that in described reative cell, temperature is 350～1200 DEG C, pressure
For-2～5kPa.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106830604A (en) * | 2017-02-27 | 2017-06-13 | 宜兴市创新环保有限公司 | Cryogenic pelletization pyrolysis installation in a kind of oily sludge |
| CN109231762A (en) * | 2018-09-21 | 2019-01-18 | 浙江天行健水务有限公司 | Sludge forming integrated machine |
| CN109609162A (en) * | 2019-01-02 | 2019-04-12 | 青岛伊克斯达智能装备有限公司 | Serialization bidirectional feed device and feed process for solid material thermal cracking |
-
2016
- 2016-08-10 CN CN201610654687.XA patent/CN106082576A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106830604A (en) * | 2017-02-27 | 2017-06-13 | 宜兴市创新环保有限公司 | Cryogenic pelletization pyrolysis installation in a kind of oily sludge |
| CN109231762A (en) * | 2018-09-21 | 2019-01-18 | 浙江天行健水务有限公司 | Sludge forming integrated machine |
| CN109231762B (en) * | 2018-09-21 | 2023-12-26 | 浙江天行健水务有限公司 | Sludge forming integrated machine |
| CN109609162A (en) * | 2019-01-02 | 2019-04-12 | 青岛伊克斯达智能装备有限公司 | Serialization bidirectional feed device and feed process for solid material thermal cracking |
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