CN106277695A - A kind of device and method of recirculating fluidized bed greasy filth Distillation recovery oil - Google Patents
A kind of device and method of recirculating fluidized bed greasy filth Distillation recovery oil Download PDFInfo
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- CN106277695A CN106277695A CN201610633918.9A CN201610633918A CN106277695A CN 106277695 A CN106277695 A CN 106277695A CN 201610633918 A CN201610633918 A CN 201610633918A CN 106277695 A CN106277695 A CN 106277695A
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- 238000004821 distillation Methods 0.000 title claims abstract description 146
- 230000003134 recirculating effect Effects 0.000 title claims abstract description 131
- 238000000034 method Methods 0.000 title claims abstract description 31
- 238000011084 recovery Methods 0.000 title claims abstract description 25
- 239000002918 waste heat Substances 0.000 claims abstract description 39
- 238000000926 separation method Methods 0.000 claims abstract description 22
- 238000012546 transfer Methods 0.000 claims abstract description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 22
- 238000006073 displacement reaction Methods 0.000 claims abstract description 15
- 239000007789 gas Substances 0.000 claims description 127
- 235000019198 oils Nutrition 0.000 claims description 72
- 238000004891 communication Methods 0.000 claims description 70
- 230000008676 import Effects 0.000 claims description 54
- 238000013459 approach Methods 0.000 claims description 38
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 34
- 239000003546 flue gas Substances 0.000 claims description 34
- 229920006395 saturated elastomer Polymers 0.000 claims description 31
- 235000019476 oil-water mixture Nutrition 0.000 claims description 24
- 239000002893 slag Substances 0.000 claims description 22
- 239000003245 coal Substances 0.000 claims description 20
- 238000001035 drying Methods 0.000 claims description 18
- 239000003500 flue dust Substances 0.000 claims description 18
- 239000002737 fuel gas Substances 0.000 claims description 18
- 239000003795 chemical substances by application Substances 0.000 claims description 13
- 238000007599 discharging Methods 0.000 claims description 13
- 239000012530 fluid Substances 0.000 claims description 10
- 238000009833 condensation Methods 0.000 claims description 8
- 230000005494 condensation Effects 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 7
- 230000018044 dehydration Effects 0.000 claims description 6
- 238000006297 dehydration reaction Methods 0.000 claims description 6
- 239000000779 smoke Substances 0.000 claims description 6
- 235000019504 cigarettes Nutrition 0.000 claims description 4
- 239000000428 dust Substances 0.000 claims description 4
- 238000001704 evaporation Methods 0.000 claims description 4
- 239000008187 granular material Substances 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 3
- 238000010025 steaming Methods 0.000 claims description 3
- 239000004744 fabric Substances 0.000 claims description 2
- 230000001112 coagulating effect Effects 0.000 claims 1
- 239000000463 material Substances 0.000 claims 1
- 238000005516 engineering process Methods 0.000 description 11
- 239000010802 sludge Substances 0.000 description 8
- 238000000197 pyrolysis Methods 0.000 description 6
- 238000003795 desorption Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000005243 fluidization Methods 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000006004 Quartz sand Substances 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 238000002076 thermal analysis method Methods 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
Classifications
-
- 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
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
-
- 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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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Mechanical Engineering (AREA)
- Hydrology & Water Resources (AREA)
- Water Supply & Treatment (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Drying Of Solid Materials (AREA)
- Treatment Of Sludge (AREA)
Abstract
The device and method of a kind of recirculating fluidized bed greasy filth Distillation recovery oil, belongs to greasy filth recovered oil technical field.Desludging pump connects with multiple-stage drier, multiple-stage drier connects with greasy filth groove, greasy filth plunger displacement pump connects with greasy filth groove, greasy filth plunger displacement pump connects with fluidized distillation room and greasy filth transfer pipeline, fluidized distillation room connects with secondary cyclone, secondary cyclone connects with multiple-stage drier, fluidized distillation room connects with recirculating fluidized bed, multiple-stage drier connects with condenser, condenser connects with oil-water separation system, condenser connects with recirculating fluidized bed, recirculating fluidized bed connects with primary cyclone, primary cyclone connects with fluidized distillation room and waste heat boiler, waste heat boiler connects with superheater, superheater connects with fluidized distillation room, superheater and high-temperature air preheater, economizer, low-temperature air preheater connects, low-temperature air preheater connects with sack cleaner.The present invention is for greasy filth Distillation recovery oil.
Description
Technical field
The present invention relates to the device and method of a kind of greasy filth Distillation recovery oil, belong to greasy filth recovered oil technical field.
Background technology
Greasy filth is the mixture of the oil, silt particle and the water that produce in oil extraction process, and moisture content is up to more than 90%, due to
Wherein contain the toxic organic compound bigger to environmental hazard, so harmless treatment must be carried out.Therefore, a kind of efficiently conjunction is found
The oil-sludge treatment technology of reason has great importance for the sustainable development in oil field.
At present, oil-sludge treatment mode both domestic and external mainly has landfill method, cured method, centrifugal separation, catalytic distillation
Method and Thermal desorption method etc..Wherein, centrifugal separation is to use more oil-sludge treatment technology, the main technique of this technology in the world
Flow process: first add chemical reagent in greasy filth and make the oil in greasy filth enter in water, subsequently greasy filth is sent in high speed centrifuge,
By centrifugal force, oil and mud are separated further.But, there is oil and separate with mud not thorough in this technology, oil-containing in isolated mud
Amount exceeds standard, and is not reaching to the most innoxious purpose.Additionally, this equipment dependence on import, investment height, also causing cannot be at home
Widespread adoption.
Due to it, Thermal desorption method extracts that oil quality is high, innoxious thoroughly, resource degree is high and the spy such as secondary pollution is little
Point, becomes most economical effective oil-sludge treatment mode.The cardinal principle of Thermal desorption technology is that greasy filth is heated to uniform temperature,
So that the hydrocarbons contained in greasy filth parses, by condensation reclaim again with.In existing Thermal desorption technology, one
As use high-temperature flue gas that resolution gas burning produces or electrical heating come for greasy filth be dried and pyrolysis provides heat, but these technology
There is certain defect, the sensible heat of thermal decomposition product fails to obtain secondary and utilizes, thus causes energy consumption high.Such as, Application No.
The patent of invention of 201310519314.8, uses rotary kiln as greasy filth thermal analysis apparatus, separates with recirculating fluidized bed separator
High temperature bed (quartz sand) as thermal source, owing to high temperature bed and greasy filth are easy in rotary kiln inwall adhesion so that greasy filth
Can not be sufficiently mixed with high temperature bed, it is impossible to ensure system stable operation.Additionally, there is pyrolysis gas (steam in this technology simultaneously
And fraction) heat fails to be obtained by, the problem such as pyrolysis system difficult sealing.Moreover, due to this system First air (80-120 DEG C)
On the low side with the temperature of secondary wind (80-150 DEG C), ignition temperature in fluid bed is unable to reach the 900-described in its patent
1200℃.The patent of invention of Application No. 201410510050.4, uses two-stage blade drier to be dried greasy filth, uses subsequently
The high-temperature flue gas that greasy filth and the burning of greasy filth pyrogenous origin incondensable gas produce is carried out in spiral pyrolysis oven as thermal source
The pyrolysis of greasy filth.There is oil-sludge treatment amount in this technology less, pyrolysis residue does not process, and the investment of two-stage blade drier
The problems such as high and power consumption is big.
Summary of the invention
It is an object of the invention to provide the device and method of a kind of recirculating fluidized bed greasy filth Distillation recovery oil, existing to solve
Oil-sludge treatment technology exists that energy consumption is high, equipment investment big, it is the highest to extract oil quality and the problem such as treating capacity is little.
The present invention with the high temperature of recirculating fluidized bed ash as thermal source, superheated steam as fluidizing agent, differential fluid bed is for steaming
Evaporate room, fractions various in greasy filth are evaporated, and be used for heating wet oil mud, it is achieved energy regenerating utilizes, finally by condensation
Device reclaims the oil water mixture evaporated, it is achieved Oil Recovery, thus greasy filth innoxious and recycling treatment are better achieved.
Realizing above-mentioned purpose, the technical scheme that the present invention takes is as follows:
Scheme one: the device of a kind of recirculating fluidized bed greasy filth Distillation recovery oil, including desludging pump, fluidized distillation room, recycle stream
Change bed, primary cyclone, waste heat boiler, superheater, high-temperature air preheater, economizer, low-temperature air preheater, wind
Room, secondary air inlet, fixed gas import, secondary cyclone, condenser, oil-water separation system, greasy filth or coal import, cylinder
Lag cooler, sack cleaner, ash silo, air-introduced machine, multiple-stage drier, greasy filth groove, greasy filth plunger displacement pump, discharge port, described fluidisation
Bed distillation chamber is differential ICFB distillation chamber；
The greasy filth inlet communication of described greasy filth delivery side of pump and multiple-stage drier, the greasy filth outlet of described multiple-stage drier with
Greasy filth groove inlet communication, the greasy filth import of described greasy filth plunger displacement pump and the greasy filth outlet of greasy filth groove, greasy filth plunger displacement pump
Greasy filth outlet connects with greasy filth import and the greasy filth transfer pipeline of fluidized distillation room respectively, described drier oil mud transfer pipeline
Outlet be arranged on greasy filth or the top of coal import of recirculating fluidized bed, the high-temperature fraction of described fluidized distillation room and water and steam
Gas outlet and the inlet communication of secondary cyclone, the outlet of described secondary cyclone and the fraction of multiple-stage drier
And steam inlet communication, the lower end of secondary cyclone is ash discharging hole, the solid discharge of fluidized distillation room and recycle stream
Fraction and the steam of changing the residue inlet communication of bed, the fraction of described multiple-stage drier and steam outlet and condenser enter
Mouth connection, the oil water mixture outlet of described condenser and the oil water mixture inlet communication of oil-water separation system, condenser
Fixed gas outlet through the fixed gas inlet communication of fixed gas transfer pipeline Yu recirculating fluidized bed, the exhanst gas outlet of recirculating fluidized bed
Connect with the gas approach of primary cyclone, the ash discharging hole of described primary cyclone lower end and fluidized distillation room
High temperature ash inlet communication, the exhanst gas outlet of primary cyclone connects with the gas approach of waste heat boiler, described waste heat
The exhanst gas outlet of boiler connects with the gas approach of superheater, the saturated vapor outlet of waste heat boiler and the saturated vapor of superheater
Inlet communication, the superheated steam outlet of superheater and the superheated steam inlet communication of fluidized distillation room, the flue gas of superheater goes out
Mouth connects with the gas approach of high-temperature air preheater, the exhanst gas outlet of described high-temperature air preheater and the flue gas of economizer
Inlet communication, high-temperature air preheater high temperature air outlet by high temperature air transfer pipeline respectively with recirculating fluidized bed bottom
Air compartment and the secondary air inlet connection of recirculating fluidized bed, the exhanst gas outlet of described economizer and low-temperature air preheater
Gas approach connects, and the exhanst gas outlet of described low-temperature air preheater connects with the gas approach of sack cleaner, described
The flue dust outlet of sack cleaner connects with ash silo, and the exhanst gas outlet of sack cleaner and air-introduced machine inlet communication are ciculation fluidized
Bed bottom is provided with discharge port, and described discharge port connects with the slag inlet of barrel slag cooler.
Device described in a kind of Utilization plan one realizes the method for recirculating fluidized bed greasy filth Distillation recovery oil, described method
Comprise the steps:
Step one: will in utilizing desludging pump that the wet oil mud that the moisture content after mechanical dehydration is 70-80% is sent into multiple-stage drier
Moisture drying is to 35-45%；
Step 2: dried greasy filth enters in greasy filth groove, uses greasy filth plunger displacement pump that dried greasy filth is sent into fluidisation subsequently
Distilling in bed distillation chamber, bottoms then send into burning in recirculating fluidized bed, the high temperature that in recirculating fluidized bed, burning produces
Flue gas carries high temperature ash and is introduced in primary cyclone, through primary cyclone isolated high temperature ash as distillation heat
It is indoor that fluidized distillation is sent in source, and the temperature that superheater produces simultaneously is that 400-500 DEG C of superheated steam is sent into as fluidizing agent
Fluidized distillation is indoor, and fluidized distillation indoor temperature is 500-600 DEG C；
Step 3: the high-temperature fraction that temperature is 500-600 DEG C and steam that greasy filth distillation produces pass through secondary cyclone
After ash disposal, being dried greasy filth as thermal source in entering multiple-stage drier, the fraction and the steam that leave multilevel drying machine enter cold
In condenser, condensation obtains oil water mixture and incoagulable fuel gas, and described oil water mixture then enters oil-water separation system
Interior isolated oil, described incoagulable fuel gas sends into recirculating fluidized bed internal combustion through the fixed gas import of recirculating fluidized bed
Burn；
Step 4: incoagulable fuel gas and the high-temperature flue gas of greasy filth bottoms burning generation in recirculating fluidized bed are taken
Band high temperature ash initially enters in primary cyclone, is directly entered fluid bed through primary cyclone isolated high temperature ash
As the heat source of greasy filth in distillation chamber, leave the high-temperature flue gas that temperature is 850-900 DEG C of primary cyclone first
Produce low-pressure saturated steam in entering waste heat boiler, in flue gas enters superheater subsequently and the low pressure produced in waste heat boiler is satisfied
With the superheated steam that steam is heated to 400-500 DEG C；
Step 5: leave the heat smoke that temperature is 600-650 DEG C of superheater pass sequentially through high-temperature air preheater, economizer with
And after low-temperature air preheater heat exchange cooling, enter qualified discharge after sack cleaner removing flue dust, isolate through sack cleaner
Flue dust then enter ash silo, meanwhile, the high temperature air that temperature is 450-550 DEG C leaving high-temperature air preheater is then distinguished
There is provided in entering recirculating fluidized bed by the secondary air inlet on the air compartment bottom recirculating fluidized bed and recirculating fluidized bed sidewall
Air needed for burning.
Scheme two: the device of a kind of recirculating fluidized bed greasy filth Distillation recovery oil, including primary oil dredge pump, two grades of desludging pumps,
Fluidized distillation room, recirculating fluidized bed, primary cyclone, waste heat boiler, superheater, high-temperature air preheater, economizer,
Low-temperature air preheater, air compartment, secondary air inlet, fixed gas import, secondary cyclone, condenser, oil-water separation system,
Greasy filth or coal import, barrel slag cooler, sack cleaner, ash silo, air-introduced machine, screw(-type) feeder, multiple-stage drier, paddle are dried
Machine, greasy filth storehouse, discharge port, described fluidized distillation room is differential ICFB distillation chamber；
The greasy filth inlet communication of described primary oil mud delivery side of pump and multiple-stage drier, the import of two grades of described desludging pumps with
The greasy filth outlet of multiple-stage drier, two grades of greasy filth delivery side of pump and the greasy filth inlet communication of blade drier, described slurry
Greasy filth outlet and the inlet communication in greasy filth storehouse of leaf drying machine, the outlet in described greasy filth storehouse respectively with the import of screw(-type) feeder
And drier oil mud transfer pipeline one end connection, the other end of described drier oil mud transfer pipeline be arranged on recirculating fluidized bed greasy filth or
The greasy filth inlet communication of the top of coal import, the outlet of described screw(-type) feeder and fluidized distillation room, described recycle stream
The exhanst gas outlet changing bed connects with the gas approach of primary cyclone, the ash discharging hole of described primary cyclone lower end
With the high temperature ash inlet communication of fluidized distillation room, the exhanst gas outlet of primary cyclone connects with the gas approach of waste heat boiler
Logical, the exhanst gas outlet of described waste heat boiler connects with the gas approach of superheater, and the saturated vapor outlet of waste heat boiler is respectively
Saturated vapor import with superheater and the saturated vapor inlet communication of blade drier, superheater superheated steam outlet with
The superheated steam inlet communication of fluidized distillation room, the high-temperature fraction of described fluidized distillation room and steam outlet and two grades
The inlet communication of cyclone separator, the outlet of described secondary cyclone and the fraction of multiple-stage drier and steam import
Connection, the lower end of secondary cyclone is ash discharging hole, the bottoms outlet of fluidized distillation room and the steaming of recirculating fluidized bed
Evaporating residue inlet communication, the fraction of described multiple-stage drier and steam outlet enter with two fractions and the steam of condenser
Mouthful one of them fraction and steam inlet communication, the fraction of described blade drier and steam outlet and condenser
Two fractions and another fraction of steam import and steam inlet communication, the oil water mixture outlet of described condenser
With the oil water mixture inlet communication of oil-water separation system, the fixed gas of condenser exports through fixed gas transfer pipeline and recycle stream
Changing the fixed gas inlet communication of bed, the exhanst gas outlet of superheater connects with the gas approach of high-temperature air preheater, described height
The exhanst gas outlet of warm air preheater connects with the gas approach of economizer, and the high temperature air outlet of high-temperature air preheater is passed through
High temperature air transfer pipeline secondary air inlet with the air compartment bottom recirculating fluidized bed and recirculating fluidized bed respectively connects, described
The exhanst gas outlet of economizer connect with the gas approach of low-temperature air preheater, the flue gas of described low-temperature air preheater goes out
Mouth connects with the gas approach of sack cleaner, and the flue dust outlet of described sack cleaner connects with ash silo, sack cleaner
Exhanst gas outlet and air-introduced machine inlet communication.Recirculating fluidized bed bottom is provided with discharge port, described discharge port and barrel slag cooler
Slag inlet connection.
Device described in a kind of Utilization plan two realizes the method for recirculating fluidized bed greasy filth Distillation recovery oil, described method
Comprise the steps:
Step one: utilize primary oil dredge pump that the wet oil mud that the moisture content after mechanical dehydration is 70-80% is sent into multiple-stage drier
Interior by moisture drying to 35-45%；
Step 2: use two grades of desludging pumps to continue moisture drying to 10-in dried greasy filth is sent into blade drier
15%, dried greasy filth granule enters greasy filth storehouse；Use screw(-type) feeder that dried greasy filth is sent into fluidized distillation subsequently
Indoor are distilled, and the high-temperature flue gas that in recirculating fluidized bed, burning produces carries high temperature ash and is introduced in primary cyclone,
Sending into fluidized distillation through primary cyclone isolated high temperature ash as distillation thermal source indoor, superheater produces simultaneously
Temperature is that 400-500 DEG C of superheated steam sends into fluidized distillation indoor as fluidizing agent, and fluidized distillation indoor temperature is
500-600℃.Distill remaining residue and then send into burning in recirculating fluidized bed；
Step 3: the high-temperature fraction that temperature is 500-600 DEG C and steam that greasy filth distillation produces pass through secondary cyclone
After ash disposal, enter in multiple-stage drier and be dried greasy filth as thermal source, leave multilevel drying machine and the fraction of blade drier and
In steam all enters condenser, condensation obtains oil water mixture and incoagulable fuel gas, and described oil water mixture then enters
Entering isolated oil in oil-water separation system, described incoagulable fuel gas is sent into through the fixed gas import of recirculating fluidized bed
Burning in recirculating fluidized bed；
Step 4: incoagulable fuel gas and the high-temperature flue gas of greasy filth bottoms burning generation in recirculating fluidized bed are taken
Band high temperature ash enters in primary cyclone, is directly entered fluidized distillation through primary cyclone isolated high temperature ash
The indoor heat source as greasy filth, the high-temperature flue gas that temperature is 850-900 DEG C leaving primary cyclone initially enters
The low-pressure saturated steam part produced in producing low-pressure saturated steam, described waste heat boiler in waste heat boiler is sent into paddle and is done
Being used for being dried greasy filth in dry machine, remainder low-pressure saturated steam then enters in superheater, utilizes flue gas will enter in superheater
Low-pressure saturated steam be heated to the superheated steam of 400-500 DEG C, as the fluidizing agent of fluidized distillation room；
Step 5: leave the heat smoke that temperature is 600-650 DEG C of superheater pass sequentially through high-temperature air preheater, economizer with
And after low-temperature air preheater heat exchange cooling, enter qualified discharge after sack cleaner removing flue dust, isolate through sack cleaner
Flue dust then enter ash silo, meanwhile, the high temperature air that temperature is 450-550 DEG C leaving high-temperature air preheater is then distinguished
There is provided in entering recirculating fluidized bed by the secondary air inlet on the air compartment bottom recirculating fluidized bed and recirculating fluidized bed sidewall
Air needed for burning.
The present invention provides the benefit that relative to prior art:
1, recirculating fluidized bed high temperature ash is used to steam as greasy filth as the thermal source of greasy filth distillation, differential ICFB distillation chamber
Evaporating equipment, high-temperature steam is as fluidizing agent, it is ensured that greasy filth is sufficiently mixed with high temperature ash, and the distilling effect of greasy filth is good, greasy filth
Middle oil steam rate reaches more than 90%.
2, the high-temperature fraction and the high-temperature vapor that use greasy filth distillation generation are dried wet oil mud, fully profit as thermal source
With the heat of greasy filth product of distillation, decrease the consumption of energy.
3, burning in the residue of greasy filth distillation sends into CFBB, realizes greasy filth while utilizing its heat
Harmless treatment completely.
Accompanying drawing explanation
Fig. 1 is the structural representation of the device scheme one of the recirculating fluidized bed greasy filth Distillation recovery oil of the present invention；
Fig. 2 is the structural representation of the device scheme two of the recirculating fluidized bed greasy filth Distillation recovery oil of the present invention.
In figure: desludging pump 1, primary oil dredge pump 1A, two grades of desludging pump 1B, greasy filth storehouse 2, fluidized distillation room 3, ciculation fluidized
Bed 4, primary cyclone 5, waste heat boiler 6, superheater 7, high-temperature air preheater 8, economizer 9, low-temperature air preheater
10, air compartment 11, secondary air inlet 12, fixed gas import 13, secondary cyclone 14, condenser 15, oil-water separation system 16,
Greasy filth or coal import 17, barrel slag cooler 18, sack cleaner 19, ash silo 20, air-introduced machine 21, discharge port 22, screw(-type) feeder
23, multiple-stage drier 24, greasy filth groove 25, greasy filth plunger displacement pump 26, blade drier 27.
Detailed description of the invention
Detailed description of the invention one: as it is shown in figure 1, the device of a kind of recirculating fluidized bed greasy filth Distillation recovery oil, including greasy filth
Pump 1, fluidized distillation room 3, recirculating fluidized bed 4, primary cyclone 5, waste heat boiler 6, superheater 7, high temperature air preheating
Device 8, economizer 9, low-temperature air preheater 10, air compartment 11, secondary air inlet 12, fixed gas (combustible gas) import 13, two grades rotation
Wind separator 14, condenser 15, oil-water separation system 16, greasy filth or coal import 17, barrel slag cooler 18, sack cleaner 19,
Ash silo 20, air-introduced machine 21, multiple-stage drier 24, greasy filth groove 25, greasy filth plunger displacement pump 26, discharge port 22, described fluidized distillation
Room 3 is differential ICFB distillation chamber；
The outlet of described desludging pump 1 and the greasy filth inlet communication of multiple-stage drier 24, the greasy filth of described multiple-stage drier 24
Outlet and greasy filth groove 25 inlet communication, the greasy filth import of described greasy filth plunger displacement pump 26 and the greasy filth outlet of greasy filth groove 25,
The greasy filth outlet of greasy filth plunger displacement pump 26 connects with greasy filth import and the greasy filth transfer pipeline of fluidized distillation room 3 respectively, described
The outlet of drier oil mud transfer pipeline be arranged on greasy filth or the top of coal import 17 of recirculating fluidized bed 4, described fluid bed steams
Evaporate the inlet communication of the high-temperature fraction of room 3 and steam outlet and secondary cyclone 14, described secondary cyclone
The fraction of the outlet of 14 and multiple-stage drier 24 and steam inlet communication, the lower end of secondary cyclone 14 is ash discharging hole,
The ash discharged is distributed into after-flame in recirculating fluidized bed 4, and the solid discharge of fluidized distillation room 3 enters with the residue of recirculating fluidized bed 4
Mouth connection, the fraction of described multiple-stage drier 24 and steam outlet and the fraction of condenser 15 and steam inlet communication,
The oil water mixture outlet of described condenser 15 and the oil water mixture inlet communication of oil-water separation system 16, condenser 15
Fixed gas outlet connects with fixed gas (combustible gas) import 13 of recirculating fluidized bed 4 through fixed gas transfer pipeline, recirculating fluidized bed 4
Exhanst gas outlet connect with the gas approach of primary cyclone 5, the ash discharging hole of described primary cyclone 5 lower end with
The gas approach of the high temperature ash inlet communication of fluidized distillation room 3, the exhanst gas outlet of primary cyclone 5 and waste heat boiler 6
Connection, the exhanst gas outlet of described waste heat boiler 6 connects with the gas approach of superheater 7, the saturated vapor outlet of waste heat boiler 6
With the saturated vapor inlet communication of superheater 7, the superheated steam outlet of superheater 7 is entered with the superheated steam of fluidized distillation room 3
Mouth connection, the exhanst gas outlet of superheater 7 connects with the gas approach of high-temperature air preheater 8, described high-temperature air preheater 8
Exhanst gas outlet connect with the gas approach of economizer 9, the outlet of the high temperature air of high-temperature air preheater 8 is defeated by high temperature air
The pipeline secondary air inlet 12 respectively with the air compartment 11 bottom recirculating fluidized bed 4 and recirculating fluidized bed 4 is sent to connect, described province
The exhanst gas outlet of coal device 9 connects with the gas approach of low-temperature air preheater 10, the flue gas of described low-temperature air preheater 10
Outlet connects with the gas approach of sack cleaner 19, and the flue dust outlet of described sack cleaner 19 connects with ash silo 20, cloth
The exhanst gas outlet of bag dust collector 19 and blower fan 21 inlet communication, recirculating fluidized bed 4 bottom is provided with discharge port 22, described discharge port
22 connect (discharging slag by barrel slag cooler 18) with the slag inlet of barrel slag cooler 18.
The concrete structure of the fluidized distillation room 3 in present embodiment is at patent of invention " a kind of gasification, distillation reaction dress
Put " disclosed in (ZL201210395220.X)；The concrete structure of multiple-stage drier 24 is in patent of invention " sludge multi-stage mummification
Device, fluidized combustion processing means and method " disclosed in (ZL201210065531.X).
Present embodiment provides the benefit that:
1, using recirculating fluidized bed 4 high temperature ash as the thermal source of greasy filth distillation, differential ICFB distillation chamber is as greasy filth
Distillation equipment, high-temperature steam is as fluidizing agent, it is ensured that greasy filth is sufficiently mixed with high temperature ash, and the distilling effect of greasy filth is good, oil
In mud, oil steam rate reaches more than 90%.
2, greasy filth is used to distill the high-temperature fraction produced and the high-temperature vapor thermal source as multiple-stage drier 24, fully
Make use of the heat of greasy filth product of distillation, decrease the consumption of energy.
3, burning in the residue of greasy filth distillation sends into recirculating fluidized bed 4, realizes the complete of greasy filth while utilizing its heat
Full harmless treatment.
Detailed description of the invention two: as it is shown in figure 1, a kind of device utilized described in detailed description of the invention one realizes ciculation fluidized
The method of bed greasy filth Distillation recovery oil, described method comprises the steps:
Step one: utilize desludging pump 1 that the wet oil mud that the moisture content after mechanical dehydration is 70-80% is sent into multiple-stage drier 24
Interior by moisture drying to 35-45%；
Step 2: dried greasy filth enters in greasy filth groove 25, uses greasy filth plunger displacement pump 26 to be sent into by dried greasy filth subsequently
Distilling in fluidized distillation room 3, bottoms then send into burning in recirculating fluidized bed 4, and in recirculating fluidized bed 4, burning produces
High-temperature flue gas carry high temperature ash and be introduced in primary cyclone 5, make through primary cyclone 5 isolated high temperature ash
Sending in fluidized distillation room 3 for distillation thermal source, the temperature that superheater 7 produces simultaneously is that 400-500 DEG C of superheated steam is as stream
Changing medium to send in fluidized distillation room 3, in fluidized distillation room 3, temperature is 500-600 DEG C；
Step 3: the high-temperature fraction that temperature is 500-600 DEG C and steam that greasy filth distillation produces pass through secondary cyclone
After 14 ash disposal, it is dried greasy filth as thermal source in entering multiple-stage drier 24, leaves fraction and the steam of multilevel drying machine 24
In entering condenser 15, condensation obtains oil water mixture and incoagulable fuel gas, and described oil water mixture then enters profit
Isolated oil in piece-rate system 16, described incoagulable fuel gas is sent into through the fixed gas import 13 of recirculating fluidized bed 4
Burning in recirculating fluidized bed 4；
Step 4: the incoagulable fuel gas in recirculating fluidized bed 4 and the high-temperature flue gas of greasy filth bottoms burning generation
Carry high temperature ash and initially enter in primary cyclone 5, be directly entered stream through primary cyclone 5 isolated high temperature ash
Change the interior heat source as greasy filth of bed distillation chamber 3, leave the high temperature cigarette that temperature is 850-900 DEG C of primary cyclone 5
Gas produces low-pressure saturated steam (pressure: 0.3-0.5MPa) in initially entering waste heat boiler 6, in flue gas enters superheater 7 subsequently
And the low-pressure saturated steam produced in waste heat boiler 6 is heated to the superheated steam of 400-500 DEG C；
Step 5: the heat smoke that temperature is 600-650 DEG C leaving superheater 7 passes sequentially through high-temperature air preheater 8, economizer
9 and low-temperature air preheater 10 heat exchange cooling after enter sack cleaner 19 remove qualified discharge after flue dust, through bag-type dust
The isolated flue dust of device 19 then enters ash silo 20, and meanwhile, the temperature leaving high-temperature air preheater 8 is 450-550 DEG C
High temperature air is the most respectively by the air compartment 11 bottom recirculating fluidized bed 4 and the secondary air inlet 12 on recirculating fluidized bed 4 sidewall
The air needed for burning is provided in entering recirculating fluidized bed 4.
Present embodiment provides the benefit that:
1, using recirculating fluidized bed 4 high temperature ash as the thermal source of greasy filth distillation, differential ICFB distillation chamber is as greasy filth
Distillation equipment, high-temperature steam is as fluidizing agent, it is ensured that greasy filth is sufficiently mixed with high temperature ash, and the distilling effect of greasy filth is good, oil
In mud, oil steam rate reaches more than 90%.
2, greasy filth is used to distill the high-temperature fraction produced and the high-temperature vapor thermal source as multiple-stage drier 24, fully
Make use of the heat of greasy filth product of distillation, decrease the consumption of energy.
3, burning in the residue of greasy filth distillation sends into recirculating fluidized bed 4, realizes the complete of greasy filth while utilizing its heat
Full harmless treatment.
Detailed description of the invention three: as it is shown in figure 1, the recirculating fluidized bed greasy filth Distillation recovery oil described in detailed description of the invention two
Method, in step 4, if in recirculating fluidized bed 4 incoagulable combustible gas and greasy filth bottoms burning produce high temperature
Flue-gas temperature does not reaches 850-900 DEG C, then add in recirculating fluidized bed 4 partially dried after greasy filth, or to ciculation fluidized
Coal is added combustion-supporting in bed 4.
Detailed description of the invention four: as in figure 2 it is shown, the device of a kind of recirculating fluidized bed greasy filth Distillation recovery oil, including one-level
Desludging pump 1A, two grades of desludging pump 1B, fluidized distillation room 3, recirculating fluidized bed 4, primary cyclone 5, waste heat boiler 6, mistakes
Hot device 7, high-temperature air preheater 8, economizer 9, low-temperature air preheater 10, air compartment 11, secondary air inlet 12, fixed gas (can
Combustion gas) import 13, secondary cyclone 14, condenser 15, oil-water separation system 16, greasy filth or coal import 17, drum slag cooling
Machine 18, sack cleaner 19, ash silo 20, air-introduced machine 21, screw(-type) feeder 23, multiple-stage drier 24, blade drier 27, greasy filth
Storehouse 2, discharge port 22, described fluidized distillation room 3 is differential ICFB distillation chamber；
The outlet of described primary oil dredge pump 1A and the greasy filth inlet communication of multiple-stage drier 24, two grades of described desludging pump 1B's
Import and the greasy filth outlet of multiple-stage drier 24, the outlet of two grades of desludging pump 1B connects with the greasy filth import of blade drier 27
Logical, the greasy filth outlet of described blade drier 27 and the inlet communication in greasy filth storehouse 2, the outlet in described greasy filth storehouse 2 respectively with
The import of screw(-type) feeder 23 and the connection of drier oil mud transfer pipeline one end, the other end of drier oil mud transfer pipeline is arranged on recycle stream
Change greasy filth or the top of coal import 17 of bed 4, the outlet of described screw(-type) feeder 23 and the greasy filth import of fluidized distillation room 3
Connection, the exhanst gas outlet of described recirculating fluidized bed 4 connects with the gas approach of primary cyclone 5, described one-level rotation
The ash discharging hole of wind separator 5 lower end and the high temperature ash inlet communication of fluidized distillation room 3, the flue gas of primary cyclone 5 goes out
Mouth connects with the gas approach of waste heat boiler 6, and the exhanst gas outlet of described waste heat boiler 6 connects with the gas approach of superheater 7,
The saturated vapor outlet of waste heat boiler 6 respectively with saturated vapor import and the saturated vapor of blade drier 27 of superheater 7
Inlet communication, the superheated steam outlet of superheater 7 and the superheated steam inlet communication of fluidized distillation room 3, described fluid bed
The inlet communication of the high-temperature fraction of distillation chamber 3 and steam outlet and secondary cyclone 14, two grades of described cyclonic separation
The fraction of the outlet of device 14 and multiple-stage drier 24 and steam inlet communication, the lower end of secondary cyclone 14 is ash discharge
Mouthful；The bottoms outlet of fluidized distillation room 3 and the bottoms inlet communication of recirculating fluidized bed 4, described multilevel drying
Two fractions of the fraction of device 24 and steam outlet and condenser 15 and one of them fraction of steam import and steam
Two fractions of inlet communication, the fraction of described blade drier 27 and steam outlet and condenser 15 and steam import
Another fraction and steam inlet communication, the oil water mixture outlet of described condenser 15 is with oil-water separation system 16
Oil water mixture inlet communication, the fixed gas outlet of condenser 15 is through the fixed gas of fixed gas transfer pipeline Yu recirculating fluidized bed 4
(combustible gas) import 13 connects, and the exhanst gas outlet of superheater 7 connects with the gas approach of high-temperature air preheater 8, described height
The exhanst gas outlet of warm air preheater 8 connects with the gas approach of economizer 9, the high temperature air outlet of high-temperature air preheater 8
By high temperature air transfer pipeline respectively with recirculating fluidized bed 4 bottom air compartment 11 and the secondary air inlet of recirculating fluidized bed 4
12 connections, the exhanst gas outlet of described economizer 9 connects with the gas approach of low-temperature air preheater 10, described Cryogenic air
The exhanst gas outlet of preheater 10 connects with the gas approach of sack cleaner 19, the outlet of the flue dust of described sack cleaner 19 with
Ash silo 20 connects, the exhanst gas outlet of sack cleaner 19 and air-introduced machine 21 inlet communication.Recirculating fluidized bed 4 bottom is provided with discharge port
22, described discharge port 22 connects (discharging slag by barrel slag cooler 18) with the slag inlet of barrel slag cooler 18.
The concrete structure of the fluidized distillation room 3 in present embodiment is at patent of invention " a kind of gasification, distillation reaction dress
Put " disclosed in (ZL201210395220.X)；The concrete structure of multiple-stage drier 24 is in patent of invention " sludge multi-stage mummification
Device, fluidized combustion processing means and method " disclosed in (ZL201210065531.X).
The beneficial effect of present embodiment:
1, using recirculating fluidized bed 4 high temperature ash as the thermal source of greasy filth distillation, differential ICFB distillation chamber is as greasy filth
Distillation equipment, high-temperature steam is as fluidizing agent, it is ensured that greasy filth is sufficiently mixed with high temperature ash, and the distilling effect of greasy filth is good, oil
In mud, oil steam rate reaches more than 90%.
2, greasy filth is used to distill the high-temperature fraction produced and the high-temperature vapor thermal source as multiple-stage drier 24, fully
Make use of the heat of greasy filth product of distillation, decrease the consumption of energy；Blade drier 27 is used to be dehydrated by greasy filth further, letter
Change the conveying of follow-up greasy filth, increase distillation chamber temperature simultaneously, improve oil steam rate.
3, burning in the residue of greasy filth distillation sends into recirculating fluidized bed 4, realizes the complete of greasy filth while utilizing its heat
Full harmless treatment.
Detailed description of the invention five: as in figure 2 it is shown, a kind of device utilized described in detailed description of the invention four realizes ciculation fluidized
The method of bed greasy filth Distillation recovery oil, described method comprises the steps:
Step one: utilize primary oil dredge pump 1A that the wet oil mud that the moisture content after mechanical dehydration is 70-80% is sent into multilevel drying
By moisture drying to 35-45% in device 24；
Step 2: use two grades of desludging pump 1B to continue by moisture drying extremely in dried greasy filth is sent into blade drier 27
10-15%, dried greasy filth granule enters greasy filth storehouse 2；Use screw(-type) feeder 23 that dried greasy filth is sent into fluidisation subsequently
Distilling in bed distillation chamber 3, the high-temperature flue gas that in recirculating fluidized bed 4, burning produces carries high temperature ash and is introduced into one cyclonic and divides
In device 5, send in fluidized distillation room 3 through primary cyclone 5 isolated high temperature ash as distillation thermal source, mistake simultaneously
The temperature that hot device 7 produces is that 400-500 DEG C of superheated steam is sent in fluidized distillation room 3 as fluidizing agent, fluidized distillation
In room 3, temperature is 500-600 DEG C.Distill remaining residue and then send into burning in recirculating fluidized bed 4；
Step 3: the high-temperature fraction that temperature is 500-600 DEG C and steam that greasy filth distillation produces pass through secondary cyclone
After 14 ash disposal, it is dried greasy filth as thermal source in entering multiple-stage drier 24, leaves multilevel drying machine 24 and blade drier 27
Fraction and steam all enter condenser 15 in condensation obtain oil water mixture and incoagulable fuel gas, described profit
Mixture then enters isolated oil in oil-water separation system 16, and described incoagulable fuel gas is through recirculating fluidized bed 4
Burning in recirculating fluidized bed 4 is sent in fixed gas import 13；
Step 4: the incoagulable fuel gas in recirculating fluidized bed 4 and the high-temperature flue gas of greasy filth bottoms burning generation
Carry high temperature ash to enter in primary cyclone 5, be directly entered fluid bed through primary cyclone 5 isolated high temperature ash
As the heat source of greasy filth in distillation chamber 3, the high-temperature flue gas that temperature is 850-900 DEG C leaving primary cyclone 5 is first
Producing low-pressure saturated steam (pressure: 0.6-1.0MPa) in being introduced into waste heat boiler 6, produce in described waste heat boiler 6 is low
A pressure saturated vapor part is used for being dried greasy filth in sending into blade drier 27, and it is overheated that remainder low-pressure saturated steam then enters
In device 7, flue gas is utilized the low-pressure saturated steam entered in superheater 7 to be heated to the superheated steam of 400-500 DEG C, as fluidisation
The fluidizing agent of bed distillation chamber 3；
Step 5: the heat smoke that temperature is 600-650 DEG C leaving superheater 7 passes sequentially through high-temperature air preheater 8, economizer
9 and low-temperature air preheater 10 heat exchange cooling after enter sack cleaner 19 remove qualified discharge after flue dust, through bag-type dust
The isolated flue dust of device 19 then enters ash silo 20, and meanwhile, the temperature leaving high-temperature air preheater 8 is 450-550 DEG C
High temperature air is the most respectively by the air compartment 11 bottom recirculating fluidized bed 4 and the secondary air inlet 12 on recirculating fluidized bed 4 sidewall
The air needed for burning is provided in entering recirculating fluidized bed 4.
The beneficial effect of present embodiment is identical with detailed description of the invention five.
Detailed description of the invention six: as in figure 2 it is shown, the recirculating fluidized bed greasy filth Distillation recovery oil described in detailed description of the invention five
Method, in step 4, if in recirculating fluidized bed 4 incoagulable combustible gas and greasy filth bottoms burning produce high temperature cigarette
Temperature does not reaches 850-900 DEG C, then add in recirculating fluidized bed 4 partially dried after greasy filth, or to recirculating fluidized bed 4
Interior interpolation coal is combustion-supporting.
Claims (6)
1. the device of a recirculating fluidized bed greasy filth Distillation recovery oil, it is characterised in that: include desludging pump (1), fluidized distillation
Room (3), recirculating fluidized bed (4), primary cyclone (5), waste heat boiler (6), superheater (7), high-temperature air preheater
(8), economizer (9), low-temperature air preheater (10), air compartment (11), secondary air inlet (12), fixed gas import (13), two grades
Cyclone separator (14), condenser (15), oil-water separation system (16), greasy filth or coal import (17), barrel slag cooler (18), cloth
Bag dust collector (19), ash silo (20), air-introduced machine (21), multiple-stage drier (24), greasy filth groove (25), greasy filth plunger displacement pump (26), unload
Material mouth (22), described fluidized distillation room (3) is differential ICFB distillation chamber；
The outlet of described desludging pump (1) and the greasy filth inlet communication of multiple-stage drier (24), described multiple-stage drier (24)
Greasy filth outlet and greasy filth groove (25) inlet communication, the greasy filth import of described greasy filth plunger displacement pump (26) and the oil of greasy filth groove (25)
Mud outlet, the greasy filth outlet of greasy filth plunger displacement pump (26) is defeated with the greasy filth import of fluidized distillation room (3) and greasy filth respectively
Pipeline connection, the outlet of described greasy filth transfer pipeline is sent to be arranged on the greasy filth of recirculating fluidized bed (4) or the upper of coal import (17)
Side, the high-temperature fraction of described fluidized distillation room (3) and steam outlet and the inlet communication of secondary cyclone (14),
The outlet of described secondary cyclone (14) and the fraction of multiple-stage drier (24) and steam inlet communication, two grades of whirlwind
The lower end of separator (14) is ash discharging hole, and the solid discharge of fluidized distillation room (3) connects with the residue import of recirculating fluidized bed (4)
Logical, the fraction of described multiple-stage drier (24) and steam outlet and the fraction of condenser (15) and steam inlet communication,
The oil water mixture outlet of described condenser (15) and the oil water mixture inlet communication of oil-water separation system (16), condenser
(15) fixed gas outlet connects with the fixed gas import (13) of recirculating fluidized bed (4) through fixed gas transfer pipeline, ciculation fluidized
The bed exhanst gas outlet of (4) connects with the gas approach of primary cyclone (5), described primary cyclone (5) lower end
The high temperature ash inlet communication of ash discharging hole and fluidized distillation room (3), the exhanst gas outlet of primary cyclone (5) and waste heat pot
The gas approach connection of stove (6), the exhanst gas outlet of described waste heat boiler (6) connects with the gas approach of superheater (7), waste heat
Saturated vapor outlet and the saturated vapor inlet communication of superheater (7) of boiler (6), the superheated steam outlet of superheater (7) with
The steam inlet connection of fluidized distillation room (3), the exhanst gas outlet of superheater (7) enters with the flue gas of high-temperature air preheater (8)
Mouth connection, the exhanst gas outlet of described high-temperature air preheater (8) connects with the gas approach of economizer (9), and high temperature air is pre-
Hot device (8) high temperature air outlet by high temperature air transfer pipeline respectively with recirculating fluidized bed (4) bottom air compartment (11) with
And secondary air inlet (12) connection of recirculating fluidized bed (4), the exhanst gas outlet of described economizer (9) and low-temperature air preheater
(10) gas approach connection, the exhanst gas outlet of described low-temperature air preheater (10) enters with the flue gas of sack cleaner (19)
Mouth connection, the flue dust outlet of described sack cleaner (19) connects with ash silo (20), the exhanst gas outlet of sack cleaner (19)
With air-introduced machine (21) inlet communication, recirculating fluidized bed (4) bottom is provided with discharge port (22), and described discharge port (22) is cold with cylinder
The slag inlet connection of slag machine (18).
2. utilizing the method that the device described in claim 1 realizes recirculating fluidized bed greasy filth Distillation recovery oil, its feature exists
In: described method comprises the steps:
Step one: utilize desludging pump (1) that the wet oil mud that the moisture content after mechanical dehydration is 70-80% is sent into multiple-stage drier
(24) by moisture drying to 35-45% in；
Step 2: dried greasy filth enters in greasy filth groove (25), uses greasy filth plunger displacement pump (26) by dried greasy filth subsequently
Distilling in sending into fluidized distillation room (3), bottoms then send into burning in recirculating fluidized bed (4), recirculating fluidized bed (4)
The high-temperature flue gas that interior burning produces carries high temperature ash and is introduced in primary cyclone (5), through primary cyclone (5) point
The high temperature ash separated out is sent in fluidized distillation room (3) as distillation thermal source, and the temperature that superheater (7) produces simultaneously is 400-
500 DEG C of superheated steams are sent in fluidized distillation room (3) as fluidizing agent, and fluidized distillation room (3) interior temperature is 500-600
℃；
Step 3: the high-temperature fraction that temperature is 500-600 DEG C and steam that greasy filth distillation produces pass through secondary cyclone
(14), after ash disposal, in entering multiple-stage drier (24), is dried greasy filth as thermal source, leave multilevel drying machine (24) fraction and
In steam enters condenser (15), condensation obtains oil water mixture and incoagulable fuel gas, and described oil water mixture is then
Enter oil-water separation system (16) interior isolated oil, described incoagulable fuel gas not coagulating through recirculating fluidized bed (4)
Gas import (13) is burned in sending into recirculating fluidized bed (4)；
Step 4: the incoagulable fuel gas in recirculating fluidized bed (4) and the high temperature cigarette of greasy filth bottoms burning generation
Gas carries high temperature ash and initially enters in primary cyclone (5), through primary cyclone (5) isolated high temperature ash directly
Entering the interior heat source as greasy filth in fluidized distillation room (3), the temperature leaving primary cyclone (5) is 850-900
DEG C high-temperature flue gas initially enter and produce low-pressure saturated steam in waste heat boiler (6), in flue gas enters superheater (7) subsequently and by
The low-pressure saturated steam produced in waste heat boiler (6) is heated to the superheated steam of 400-500 DEG C；
Step 5: the heat smoke that temperature is 600-650 DEG C leaving superheater (7) passes sequentially through high-temperature air preheater (8), saves
Qualified discharge after sack cleaner (19) removing flue dust is entered after coal device (9) and low-temperature air preheater (10) heat exchange cooling,
Then enter ash silo (20) through sack cleaner (19) isolated flue dust, meanwhile, leave the temperature of high-temperature air preheater (8)
The high temperature air that degree is 450-550 DEG C is the most respectively by air compartment (11) and the recirculating fluidized bed (4) of recirculating fluidized bed (4) bottom
Secondary air inlet (12) on sidewall provides the air needed for burning in entering recirculating fluidized bed (4).
The method of recirculating fluidized bed greasy filth Distillation recovery the most according to claim 2 oil, it is characterised in that: in step 4,
If the high-temperature flue-gas that in recirculating fluidized bed (4), incoagulable combustible gas and the burning of greasy filth bottoms produce reaches not
To 850-900 DEG C, then the greasy filth after interpolation is partially dried in recirculating fluidized bed (4), or add in recirculating fluidized bed (4)
Coal comes combustion-supporting.
4. the device of recirculating fluidized bed greasy filth Distillation recovery oil, it is characterised in that: include primary oil dredge pump (1A), two grades
Desludging pump (1B), fluidized distillation room (3), recirculating fluidized bed (4), primary cyclone (5), waste heat boiler (6), superheater
(7), high-temperature air preheater (8), economizer (9), low-temperature air preheater (10), air compartment (11), secondary air inlet (12), no
Solidifying gas import (13), secondary cyclone (14), condenser (15), oil-water separation system (16), greasy filth or coal import (17),
Barrel slag cooler (18), sack cleaner (19), ash silo (20), air-introduced machine (21), screw(-type) feeder (23), multiple-stage drier
(24), blade drier (27), greasy filth storehouse (2), discharge port (22), described fluidized distillation room (3) is differential inner recirculation flow
Change bed distillation chamber；
The outlet of described primary oil dredge pump (1A) and the greasy filth inlet communication of multiple-stage drier (24), two grades of described desludging pumps
(1B) import and the greasy filth outlet of multiple-stage drier (24), the outlet of two grades of desludging pumps (1B) and blade drier (27)
Greasy filth inlet communication, greasy filth outlet and the inlet communication in greasy filth storehouse (2), the described greasy filth of described blade drier (27)
The outlet in storehouse (2) connects with import and drier oil mud transfer pipeline one end of screw(-type) feeder (23) respectively, and described drier oil mud is defeated
The other end sending pipeline is arranged on greasy filth or the top of coal import (17), the described screw(-type) feeder of recirculating fluidized bed (4)
(23) outlet and the greasy filth inlet communication of fluidized distillation room (3), the exhanst gas outlet of described recirculating fluidized bed (4) and one-level
The gas approach connection of cyclone separator (5), the ash discharging hole of described primary cyclone (5) lower end and fluidized distillation room
(3) high temperature ash inlet communication, the exhanst gas outlet of primary cyclone (5) connects with the gas approach of waste heat boiler (6), institute
The exhanst gas outlet of the waste heat boiler (6) stated connects with the gas approach of superheater (7), the saturated vapor outlet of waste heat boiler (6)
Respectively with saturated vapor import and the saturated vapor inlet communication of blade drier (27) of superheater (7), superheater (7)
Superheated steam outlet and the superheated steam inlet communication of fluidized distillation room (3), the high temperature of described fluidized distillation room (3) evaporates
Point and the inlet communication of steam outlet and secondary cyclone (14), the outlet of described secondary cyclone (14) with
The fraction of multiple-stage drier (24) and steam inlet communication, the lower end of secondary cyclone (14) is ash discharging hole, fluid bed
The bottoms outlet of distillation chamber (3) and the bottoms inlet communication of recirculating fluidized bed (4), described multiple-stage drier (24)
Fraction and two fractions of steam outlet and condenser (15) and one of them fraction of steam import and steam enter
Mouthful connection, the fraction of described blade drier (27) and steam outlet enter with two fractions and the steam of condenser (15)
Another fraction of mouth and steam inlet communication, the oil water mixture outlet of described condenser (15) and oil-water separation system
(16) oil water mixture inlet communication, the fixed gas of condenser (15) exports through fixed gas transfer pipeline and recirculating fluidized bed
(4) fixed gas import 13 connects, and the exhanst gas outlet of superheater (7) connects with the gas approach of high-temperature air preheater (8), institute
The exhanst gas outlet of the high-temperature air preheater (8) stated connects with the gas approach of economizer (9), high-temperature air preheater (8)
High temperature air outlet by high temperature air transfer pipeline respectively with the air compartment (11) and ciculation fluidized of recirculating fluidized bed (4) bottom
Secondary air inlet (12) connection of bed (4), the exhanst gas outlet of described economizer (9) and the flue gas of low-temperature air preheater (10)
Inlet communication, the exhanst gas outlet of described low-temperature air preheater (10) connects with the gas approach of sack cleaner (19), institute
The flue dust outlet of the sack cleaner (19) stated connects with ash silo (20), the exhanst gas outlet of sack cleaner (19) and air-introduced machine
(21) inlet communication, recirculating fluidized bed (4) bottom is provided with discharge port (22), described discharge port (22) and barrel slag cooler (18)
Slag inlet connection.
5. utilizing the method that the device described in claim 4 realizes recirculating fluidized bed greasy filth Distillation recovery oil, its feature exists
In: described method comprises the steps:
Step one: utilize primary oil dredge pump (1A) to be sent into by the wet oil mud that the moisture content after mechanical dehydration is 70-80% multistage dry
By moisture drying to 35-45% in dry device (24)；
Step 2: use two grades of desludging pumps (1B) to continue moisture drying in dried greasy filth is sent into blade drier (27)
To 10-15%, dried greasy filth granule enters greasy filth storehouse (2)；Screw(-type) feeder (23) is used to be sent by dried greasy filth subsequently
Fluidized bed distillation chamber distills in (3), and the high-temperature flue gas that in recirculating fluidized bed (4), burning produces carries high temperature ash and is introduced into
In primary cyclone (5), send into fluid bed through primary cyclone (5) isolated high temperature ash as distillation thermal source and steam
Evaporating in room (3), the temperature that superheater (7) produces simultaneously is that 400-500 DEG C of superheated steam sends into fluid bed steaming as fluidizing agent
Evaporating in room (3), fluidized distillation room (3) interior temperature is 500-600 DEG C, distills remaining residue and then sends into recirculating fluidized bed (4)
Interior burning；
Step 3: the high-temperature fraction that temperature is 500-600 DEG C and steam that greasy filth distillation produces pass through secondary cyclone
(14) after ash disposal, in entering multiple-stage drier (24), it is dried greasy filth as thermal source, leaves multilevel drying machine (24) and paddle is done
In the fraction of dry machine (27) and steam all enter condenser (15), condensation obtains oil water mixture and incoagulable fuel gas,
Described oil water mixture then enters oil-water separation system (16) interior isolated oil, and described incoagulable fuel gas is through following
Burning in recirculating fluidized bed (4) is sent in the fixed gas import (13) of ring fluid bed (4)；
Step 4: the incoagulable fuel gas in recirculating fluidized bed (4) and the high temperature cigarette of greasy filth bottoms burning generation
Gas carries high temperature ash and enters in primary cyclone (5), is directly entered through primary cyclone (5) isolated high temperature ash
As the heat source of greasy filth in fluidized distillation room (3), the temperature leaving primary cyclone (5) is 850-900 DEG C
High-temperature flue gas produces the low pressure produced in low-pressure saturated steam, described waste heat boiler (6) and satisfies in initially entering waste heat boiler (6)
Being used for being dried greasy filth in sending into blade drier (27) with a steam part, remainder low-pressure saturated steam then enters superheater
(7), in, flue gas is utilized the low-pressure saturated steam entered in superheater (7) to be heated to the superheated steam of 400-500 DEG C, as stream
Change the fluidizing agent of bed distillation chamber (3)；
Step 5: the heat smoke that temperature is 600-650 DEG C leaving superheater (7) passes sequentially through high-temperature air preheater (8), saves
Qualified discharge after sack cleaner (19) removing flue dust is entered after coal device (9) and low-temperature air preheater (10) heat exchange cooling,
Then enter ash silo (20) through sack cleaner (19) isolated flue dust, meanwhile, leave the temperature of high-temperature air preheater (8)
The high temperature air that degree is 450-550 DEG C is the most respectively by air compartment (11) and the recirculating fluidized bed (4) of recirculating fluidized bed (4) bottom
Secondary air inlet (12) on sidewall provides the air needed for burning in entering recirculating fluidized bed (4).
The method of recirculating fluidized bed greasy filth Distillation recovery the most according to claim 5 oil, it is characterised in that: in step 4,
If the high-temperature flue-gas that in recirculating fluidized bed (4), incoagulable combustible gas and the burning of greasy filth bottoms produce reaches not
To 850-900 DEG C, then the greasy filth after interpolation is partially dried in recirculating fluidized bed (4), or add in recirculating fluidized bed (4)
Coal comes combustion-supporting.
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| CN112827202A (en) * | 2020-12-30 | 2021-05-25 | 肥城金塔酒精化工设备有限公司 | A fuel ethanol distillation method and device using the secondary steam of a superheated steam fluidized bed dryer as part of the heat source |
| CN113587114A (en) * | 2021-07-30 | 2021-11-02 | 北京工商大学 | High-water-content oil sludge clean combustion treatment device |
| CN114940570A (en) * | 2022-07-11 | 2022-08-26 | 四川龙锦宇科技有限公司 | Oil-containing sludge deoiling and dewatering device, process and application |
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| CN112827202A (en) * | 2020-12-30 | 2021-05-25 | 肥城金塔酒精化工设备有限公司 | A fuel ethanol distillation method and device using the secondary steam of a superheated steam fluidized bed dryer as part of the heat source |
| CN112779057A (en) * | 2020-12-31 | 2021-05-11 | 上海电气集团股份有限公司 | Comprehensive oil sludge treatment system and comprehensive oil sludge treatment method |
| CN113587114A (en) * | 2021-07-30 | 2021-11-02 | 北京工商大学 | High-water-content oil sludge clean combustion treatment device |
| CN114940570A (en) * | 2022-07-11 | 2022-08-26 | 四川龙锦宇科技有限公司 | Oil-containing sludge deoiling and dewatering device, process and application |
| CN114940570B (en) * | 2022-07-11 | 2023-03-07 | 四川龙锦宇科技有限公司 | Oil-containing sludge deoiling and dewatering device, process and application |
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