CN106277695B - Device and method for recovering oil by circulating fluidized bed oil sludge distillation - Google Patents
Device and method for recovering oil by circulating fluidized bed oil sludge distillation Download PDFInfo
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- CN106277695B CN106277695B CN201610633918.9A CN201610633918A CN106277695B CN 106277695 B CN106277695 B CN 106277695B CN 201610633918 A CN201610633918 A CN 201610633918A CN 106277695 B CN106277695 B CN 106277695B
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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
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
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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
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- 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
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- 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
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- 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
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Abstract
A device and a method for recovering oil by circulating fluidized bed oil sludge distillation belong to the technical field of oil sludge recovered oil. The oil sludge pump is communicated with the multistage dryer, the multistage dryer is communicated with the oil sludge tank, the oil sludge plunger pump is communicated with the fluidized bed distillation chamber and an oil sludge conveying pipeline, the fluidized bed distillation chamber is communicated with the secondary cyclone separator, the secondary cyclone separator is communicated with the multistage dryer, the fluidized bed distillation chamber is communicated with the circulating fluidized bed, the multistage dryer is communicated with the condenser, the condenser is communicated with the oil-water separation system, the condenser is communicated with the circulating fluidized bed, the circulating fluidized bed is communicated with the primary cyclone separator, the primary cyclone separator is communicated with the fluidized bed distillation chamber and the waste heat boiler, the waste heat boiler is communicated with the superheater, the superheater is communicated with the fluidized bed distillation chamber, the superheater is communicated with the high-temperature air preheater, the economizer and the low-temperature air preheater is communicated with the bag-type dust collector. The invention is used for recovering oil by distilling oil sludge.
Description
Technical Field
The invention relates to a device and a method for recovering oil by distilling oil sludge, belonging to the technical field of oil sludge recovered oil.
Background
The oil sludge is a mixture of oil, sand and water generated in the process of oil field exploitation, the water content is up to more than 90 percent, and the oil sludge contains toxic organic matters which are harmful to the environment, so the oil sludge needs to be subjected to harmless treatment. Therefore, the search for an efficient and reasonable oil sludge treatment technology has important significance for the sustainable development of the oil field.
At present, the treatment modes of oil sludge at home and abroad mainly comprise a landfill method, a solidification treatment method, a centrifugal separation method, a catalytic distillation method, a thermal desorption method and the like. The centrifugal separation method is an oil sludge treatment technology which is used more internationally, and the main process flow of the technology is as follows: firstly, adding chemical reagent into the oil sludge to enable the oil in the oil sludge to enter water, then sending the oil sludge into a high-speed centrifuge, and further separating the oil from the sludge through centrifugal force. However, the technology has the defects that the oil and the mud are not completely separated, the oil content in the separated mud exceeds the standard, and the purpose of thorough harmless treatment is not achieved. In addition, the equipment depends on import, has high investment and cannot be widely applied in China.
The thermal desorption method is the most economic and effective oil sludge treatment method due to the characteristics of high quality of extracted oil, thorough harmlessness, high resource degree, small secondary pollution and the like. The main principle of the thermal desorption technology is that the oil sludge is heated to a certain temperature, so that hydrocarbon substances contained in the oil sludge are desorbed and then condensed and recycled. In the existing thermal desorption technology, high-temperature flue gas generated by combustion of desorption gas or electric heating is generally adopted to provide heat for drying and pyrolysis of oil sludge, but the technologies have certain defects, and sensible heat of pyrolysis products cannot be reused, so that energy consumption is high. For example, in the patent of patent application No. 201310519314.8, a rotary kiln is used as a device for analyzing thermal oil sludge, high-temperature bed materials (quartz sand) separated by a circulating fluidized bed separator are used as a heat source, and the high-temperature bed materials and oil sludge are easily adhered to each other on the inner wall of the rotary kiln, so that the oil sludge and the high-temperature bed materials cannot be sufficiently mixed, and the stable operation of a system cannot be ensured. In addition, the technology has the problems that the heat of pyrolysis gas (water vapor and fraction) cannot be utilized, the sealing of a pyrolysis system is difficult, and the like. Moreover, the temperature of the primary air (80-120 ℃) and the secondary air (80-150 ℃) of the system is low, so that the combustion temperature in the fluidized bed can not reach 900-1200 ℃ as described in the patent. The invention patent with the application number of 201410510050.4 uses a two-stage paddle dryer to dry oil sludge, and then uses high-temperature flue gas generated by combustion of non-condensable gas generated by oil sludge pyrolysis as a heat source to carry out pyrolysis of the oil sludge in a spiral pyrolysis furnace. The technology has the problems of small oil sludge treatment capacity, no treatment of pyrolysis slag, high investment and large power consumption of a two-stage paddle dryer and the like.
Disclosure of Invention
The invention aims to provide a device and a method for recovering oil by distilling oil sludge in a circulating fluidized bed, which aim to solve the problems of high energy consumption, large equipment investment, low quality of extracted oil, small treatment capacity and the like in the existing oil sludge treatment technology.
According to the invention, the high-temperature ash of the circulating fluidized bed is used as a heat source, superheated steam is used as a fluidizing medium, and the differential fluidized bed is used as a distillation chamber, so that various fractions in the oil sludge are evaporated and used for heating wet oil sludge to realize energy recycling, and finally, the evaporated oil-water mixture is recycled through the condenser to realize oil recovery, thereby better realizing harmless and resource treatment of the oil sludge.
The technical scheme adopted by the invention is as follows:
the first scheme comprises the following steps: a device for recovering oil by distillation of oil sludge in a circulating fluidized bed comprises an oil sludge pump, a fluidized bed distillation chamber, a circulating fluidized bed, a primary cyclone separator, a waste heat boiler, a superheater, a high-temperature air preheater, an economizer, a low-temperature air preheater, an air chamber, a secondary air inlet, a non-condensable gas inlet, a secondary cyclone separator, a condenser, an oil-water separation system, oil sludge or coal inlets, a roller slag cooler, a bag-type dust remover, an ash bin, an induced draft fan, a multistage dryer, an oil sludge groove, an oil sludge plunger pump and a discharge opening, wherein the fluidized bed distillation chamber is a differential internal circulating fluidized bed distillation chamber;
the outlet of the oil sludge pump is communicated with the oil sludge inlet of the multistage dryer, the oil sludge outlet of the multistage dryer is communicated with the oil sludge groove inlet, the oil sludge inlet of the oil sludge plunger pump is communicated with the oil sludge outlet of the oil sludge groove, the oil sludge outlet of the oil sludge plunger pump is respectively communicated with the oil sludge inlet of the fluidized bed distillation chamber and the oil sludge conveying pipeline, the outlet of the dry oil sludge conveying pipeline is arranged above the oil sludge or coal inlet of the circulating fluidized bed, the high-temperature fraction and steam outlet of the fluidized bed distillation chamber is communicated with the inlet of the secondary cyclone separator, the outlet of the secondary cyclone separator is communicated with the fraction and steam inlet of the multistage dryer, the lower end of the secondary cyclone separator is an ash discharge port, the residue outlet of the fluidized bed distillation chamber is communicated with the residue inlet of the circulating fluidized bed, and the fraction and steam outlet of the multistage dryer are communicated with the fraction and steam inlet of the condenser, an oil-water mixture outlet of the condenser is communicated with an oil-water mixture inlet of an oil-water separation system, a noncondensable gas outlet of the condenser is communicated with a noncondensable gas inlet of a circulating fluidized bed through a noncondensable gas conveying pipeline, a flue gas outlet of the circulating fluidized bed is communicated with a flue gas inlet of a primary cyclone separator, an ash discharge port at the lower end of the primary cyclone separator is communicated with a high-temperature ash inlet of a distillation chamber of the fluidized bed, a flue gas outlet of the primary cyclone separator is communicated with a flue gas inlet of a waste heat boiler, a flue gas outlet of the waste heat boiler is communicated with a flue gas inlet of a superheater, a saturated steam outlet of the waste heat boiler is communicated with a saturated steam inlet of the superheater, a superheated steam outlet of the superheater is communicated with a superheated steam inlet of the distillation chamber of the fluidized bed, and a flue gas outlet of the superheater is communicated with a flue gas inlet of a high-temperature air preheater, the flue gas outlet of high temperature air heater and economizer's flue gas inlet intercommunication, high temperature air heater's high temperature air outlet pass through high temperature air conveying line respectively with the plenum of circulating fluidized bed bottom and circulating fluidized bed's overgrate air import intercommunication, economizer's flue gas outlet and low temperature air heater's flue gas inlet intercommunication, low temperature air heater's flue gas outlet and sack cleaner's flue gas inlet intercommunication, the smoke and dust export and the ash bin intercommunication of sack cleaner, the flue gas outlet and the draught fan import intercommunication of sack cleaner, the circulating fluidized bed lower part is equipped with the discharge opening, discharge opening and the slag inlet intercommunication of cylinder cold sediment machine.
A method for recovering oil by performing circulating fluidized bed sludge distillation using the apparatus of scheme one, the method comprising the steps of:
the method comprises the following steps: sending wet oil sludge with the water content of 70-80 percent after mechanical dehydration into a multistage dryer by using an oil sludge pump to dry the water content to 35-45 percent;
step two: the dried oil sludge enters an oil sludge groove, then the dried oil sludge is fed into a fluidized bed distillation chamber for distillation by using an oil sludge plunger pump, distillation residues are fed into a circulating fluidized bed for combustion, high-temperature flue gas generated by combustion in the circulating fluidized bed carries high-temperature ash to enter a primary cyclone separator, the high-temperature ash separated by the primary cyclone separator is used as a distillation heat source to be fed into the fluidized bed distillation chamber, meanwhile, superheated steam generated by a superheater and having the temperature of 400-500 ℃ is used as a fluidizing medium to be fed into the fluidized bed distillation chamber, and the temperature in the fluidized bed distillation chamber is 500-600 ℃;
step three: high-temperature fractions and steam which are generated by distillation of oil sludge and have the temperature of 500-600 ℃ are dedusted by a secondary cyclone separator, the oil sludge is dried by entering a multistage dryer as a heat source, the fractions and the steam which leave the multistage dryer enter a condenser to be condensed to obtain an oil-water mixture and uncondensed combustible gas, the oil-water mixture enters an oil-water separation system to be separated to obtain oil, and the uncondensed combustible gas is fed into a circulating fluidized bed through an uncondensed gas inlet of the circulating fluidized bed to be combusted;
step four: the method comprises the following steps that non-condensable combustible gas in a circulating fluidized bed and high-temperature flue gas generated by combustion of oil sludge distillation residues carry high-temperature ash to enter a primary cyclone separator, the high-temperature ash separated by the primary cyclone separator directly enters a fluidized bed distillation chamber to serve as a heating source of oil sludge, the high-temperature flue gas leaving the primary cyclone separator and having the temperature of 850-900 ℃ firstly enters a waste heat boiler to generate low-pressure saturated steam, and then the flue gas enters a superheater and heats the low-pressure saturated steam generated in the waste heat boiler to superheated steam of 400-500 ℃;
step five: the hot flue gas leaving the superheater and having the temperature of 600-650 ℃ is subjected to heat exchange and temperature reduction through the high-temperature air preheater, the economizer and the low-temperature air preheater and then enters the bag-type dust remover to remove smoke dust, the smoke dust separated by the bag-type dust remover is discharged after reaching standards, and meanwhile, the high-temperature air leaving the high-temperature air preheater and having the temperature of 450-550 ℃ enters the circulating fluidized bed through the air chamber at the bottom of the circulating fluidized bed and the secondary air inlet on the side wall of the circulating fluidized bed respectively to provide air required by combustion.
Scheme two is as follows: a device for recovering oil by distilling circulating fluidized bed sludge comprises a primary sludge pump, a secondary sludge pump, a fluidized bed distillation chamber, a circulating fluidized bed, a primary cyclone separator, a waste heat boiler, a superheater, a high-temperature air preheater, a coal economizer, a low-temperature air preheater, an air chamber, a secondary air inlet, a non-condensable gas inlet, a secondary cyclone separator, a condenser, an oil-water separation system, a sludge or coal inlet, a roller slag cooler, a bag-type dust remover, an ash bin, an induced draft fan, a screw feeder, a multi-stage dryer, a blade dryer, a sludge bin and a discharge opening, wherein the fluidized bed distillation chamber is a differential internal circulating fluidized bed distillation chamber;
the outlet of the first-stage oil sludge pump is communicated with the oil sludge inlet of the multi-stage dryer, the inlet of the second-stage oil sludge pump is communicated with the oil sludge outlet of the multi-stage dryer, the outlet of the second-stage oil sludge pump is communicated with the oil sludge inlet of the paddle dryer, the oil sludge outlet of the paddle dryer is communicated with the inlet of the oil sludge bin, the outlet of the oil sludge bin is respectively communicated with the inlet of the screw feeder and one end of a dry oil sludge conveying pipeline, the other end of the dry oil sludge conveying pipeline is arranged above the oil sludge or coal inlet of the circulating fluidized bed, the outlet of the screw feeder is communicated with the oil sludge inlet of the fluidized bed distillation chamber, the flue gas outlet of the circulating fluidized bed is communicated with the flue gas inlet of the first-stage cyclone separator, the ash discharge port at the lower end of the first-stage cyclone separator is communicated with the high-temperature ash inlet of the fluidized bed distillation chamber, and the flue gas outlet of the first-stage cyclone separator is communicated with the flue gas inlet of the waste heat boiler, the flue gas outlet of the waste heat boiler is communicated with the flue gas inlet of the superheater, the saturated steam outlet of the waste heat boiler is respectively communicated with the saturated steam inlet of the superheater and the saturated steam inlet of the paddle dryer, the superheated steam outlet of the superheater is communicated with the superheated steam inlet of the fluidized bed distillation chamber, the high-temperature fraction and steam outlet of the fluidized bed distillation chamber is communicated with the inlet of the secondary cyclone separator, the outlet of the secondary cyclone separator is communicated with the fraction and steam inlet of the multistage dryer, the lower end of the secondary cyclone separator is provided with an ash discharge port, the distillation residue outlet of the fluidized bed distillation chamber is communicated with the distillation residue inlet of the circulating fluidized bed, the fraction and steam outlet of the multistage dryer is communicated with one of the two fractions of the condenser and the steam inlet, the distillate and steam outlet of the paddle dryer is communicated with the other distillate and steam inlet of the two distillates and steam inlets of the condenser, the oil-water mixture outlet of the condenser is communicated with the oil-water mixture inlet of the oil-water separation system, the non-condensable gas outlet of the condenser is communicated with the non-condensable gas inlet of the circulating fluidized bed through a non-condensable gas conveying pipeline, the flue gas outlet of the superheater is communicated with the flue gas inlet of the high-temperature air preheater, the flue gas outlet of the high-temperature air preheater is communicated with the flue gas inlet of the economizer, the high temperature air outlet of the high temperature air preheater is respectively communicated with the air chamber at the bottom of the circulating fluidized bed and the secondary air inlet of the circulating fluidized bed through a high temperature air conveying pipeline, the flue gas outlet of the economizer is communicated with the flue gas inlet of the low temperature air preheater, the flue gas outlet of the low temperature air preheater is communicated with the flue gas inlet of the bag-type dust remover, the smoke outlet of the bag-type dust remover is communicated with the ash bin, and the flue gas outlet of the bag-type dust remover is communicated with the inlet of the draught fan. The lower part of the circulating fluidized bed is provided with a discharge port which is communicated with a slag inlet of the roller slag cooler.
A method for recovering oil by distillation of sludge in a circulating fluidized bed by using the device in the second scheme, wherein the method comprises the following steps:
the method comprises the following steps: sending the wet oil sludge with the water content of 70-80% after mechanical dehydration into a multistage dryer by using a first-stage oil sludge pump to dry the water content to 35-45%;
step two: feeding the dried oil sludge into a blade dryer by using a secondary oil sludge pump to continuously dry the water to 10-15%, and feeding the dried oil sludge particles into an oil sludge bin; and then, feeding the dried oil sludge into a fluidized bed distillation chamber by using a screw feeder for distillation, feeding high-temperature smoke gas generated by combustion in a circulating fluidized bed into a primary cyclone separator, feeding the high-temperature smoke gas into the fluidized bed distillation chamber by using the high-temperature smoke gas as a distillation heat source, wherein the high-temperature smoke gas is separated by the primary cyclone separator, the high-temperature smoke gas is fed into the fluidized bed distillation chamber by using superheated steam with the temperature of 400-500 ℃ generated by a superheater as a fluidizing medium, and the temperature in the fluidized bed distillation chamber is 500-600 ℃. The residue left after distillation is sent into a circulating fluidized bed for combustion;
step three: high-temperature fractions and steam which are generated by distillation of oil sludge and have the temperature of 500-600 ℃ are dedusted by a secondary cyclone separator, the high-temperature fractions and the steam enter a multistage dryer to be used as heat sources for drying the oil sludge, the fractions and the steam which leave the multistage dryer and a blade dryer both enter a condenser to be condensed to obtain an oil-water mixture and uncondensed combustible gas, the oil-water mixture enters an oil-water separation system to be separated to obtain oil, and the uncondensed combustible gas is fed into a circulating fluidized bed through an uncondensed gas inlet of the circulating fluidized bed to be combusted;
step four: the method comprises the following steps that non-condensable combustible gas in a circulating fluidized bed and high-temperature flue gas generated by combustion of oil sludge distillation residues carry high-temperature ash to enter a primary cyclone separator, the high-temperature ash separated by the primary cyclone separator directly enters a fluidized bed distillation chamber to serve as a heating source of oil sludge, the high-temperature flue gas leaving the primary cyclone separator and having the temperature of 850-900 ℃ firstly enters a waste heat boiler to generate low-pressure saturated steam, one part of the low-pressure saturated steam generated in the waste heat boiler is sent into a blade dryer to be used for drying the oil sludge, the rest part of the low-pressure saturated steam enters a superheater, and the low-pressure saturated steam entering the superheater is heated to 400-500 ℃ by utilizing the flue gas to serve as a fluidized medium of the fluidized bed distillation chamber;
step five: the hot flue gas leaving the superheater and having the temperature of 600-650 ℃ is subjected to heat exchange and temperature reduction through the high-temperature air preheater, the economizer and the low-temperature air preheater and then enters the bag-type dust remover to remove smoke dust, the smoke dust separated by the bag-type dust remover is discharged after reaching standards, and meanwhile, the high-temperature air leaving the high-temperature air preheater and having the temperature of 450-550 ℃ enters the circulating fluidized bed through the air chamber at the bottom of the circulating fluidized bed and the secondary air inlet on the side wall of the circulating fluidized bed respectively to provide air required by combustion.
Compared with the prior art, the invention has the beneficial effects that:
1. the high-temperature ash of the circulating fluidized bed is used as a heat source for distilling the oil sludge, the differential internal circulating fluidized bed distillation chamber is used as oil sludge distillation equipment, high-temperature steam is used as a fluidizing medium, the oil sludge and the high-temperature ash are fully mixed, the distillation effect of the oil sludge is good, and the evaporation rate of oil in the oil sludge reaches over 90 percent.
2. The wet oil sludge is dried by using high-temperature fractions generated by oil sludge distillation and high-temperature steam as heat sources, so that the heat of oil sludge distillation products is fully utilized, and the energy consumption is reduced.
3. The residue of the oil sludge distillation is sent into a circulating fluidized bed boiler for combustion, and the complete harmless treatment of the oil sludge is realized while the heat of the oil sludge is utilized.
Drawings
FIG. 1 is a schematic diagram of a first embodiment of an apparatus for recovering oil by distillation of sludge in a circulating fluidized bed according to the present invention;
fig. 2 is a schematic configuration diagram of a second embodiment of the apparatus for recovering oil by sludge distillation in a circulating fluidized bed according to the present invention.
In the figure: the system comprises a sludge pump 1, a primary sludge pump 1A, a secondary sludge pump 1B, a sludge bin 2, a fluidized bed distillation chamber 3, a circulating fluidized bed 4, a primary cyclone separator 5, a waste heat boiler 6, a superheater 7, a high-temperature air preheater 8, an economizer 9, a low-temperature air preheater 10, an air chamber 11, a secondary air inlet 12, a non-condensable gas inlet 13, a secondary cyclone separator 14, a condenser 15, an oil-water separation system 16, a sludge or coal inlet 17, a roller slag cooler 18, a bag-type dust remover 19, an ash bin 20, an induced draft fan 21, a discharge opening 22, a spiral feeder 23, a multi-stage dryer 24, a sludge tank 25, a sludge plunger pump 26 and a blade dryer 27.
Detailed Description
The first specific implementation way is as follows: as shown in fig. 1, a device for recovering oil by distillation of circulating fluidized bed sludge comprises a sludge pump 1, a fluidized bed distillation chamber 3, a circulating fluidized bed 4, a primary cyclone separator 5, a waste heat boiler 6, a superheater 7, a high temperature air preheater 8, an economizer 9, a low temperature air preheater 10, an air chamber 11, a secondary air inlet 12, a non-condensable gas (combustible gas) inlet 13, a secondary cyclone separator 14, a condenser 15, an oil-water separation system 16, a sludge or coal inlet 17, a roller slag cooler 18, a bag-type dust remover 19, an ash bin 20, an induced draft fan 21, a multistage dryer 24, a sludge tank 25, a sludge plunger pump 26 and a discharge opening 22, wherein the fluidized bed distillation chamber 3 is a differential internal circulating fluidized bed distillation chamber;
the outlet of the oil sludge pump 1 is communicated with the oil sludge inlet of a multi-stage dryer 24, the oil sludge outlet of the multi-stage dryer 24 is communicated with the inlet of an oil sludge tank 25, the oil sludge inlet of an oil sludge plunger pump 26 is communicated with the oil sludge outlet of the oil sludge tank 25, the oil sludge outlet of the oil sludge plunger pump 26 is respectively communicated with the oil sludge inlet of a fluidized bed distillation chamber 3 and an oil sludge conveying pipeline, the outlet of the dry oil sludge conveying pipeline is arranged above the oil sludge or coal inlet 17 of the circulating fluidized bed 4, the high-temperature fraction and water vapor outlet of the fluidized bed distillation chamber 3 is communicated with the inlet of a secondary cyclone separator 14, the outlet of the secondary cyclone separator 14 is communicated with the fraction and water vapor inlet of the multi-stage dryer 24, the lower end of the secondary cyclone separator 14 is an ash discharge port, the discharged ash is conveyed into the circulating fluidized bed 4 to be burned out, the residue outlet of the fluidized bed distillation chamber 3 is communicated with the residue inlet of the circulating fluidized bed 4, the fraction and water vapor outlet of the multi-stage dryer 24 is communicated with the fraction and water vapor inlet of a condenser 15, the mixture outlet of the condenser 15 is communicated with the waste heat recovery steam superheater, the waste heat recovery boiler 5 of the circulating fluidized bed condenser 6, the waste heat recovery boiler is not communicated with the waste heat recovery boiler 5, the waste heat recovery steam condenser 6, the waste heat recovery boiler 7 is communicated with the waste heat recovery steam condenser 6, the waste heat recovery boiler 4, the waste heat recovery boiler 5, the waste heat recovery boiler 7 is not communicated with the waste heat recovery boiler 5, the waste heat recovery steam condenser 6, the waste heat recovery boiler 7 is communicated with the waste heat recovery boiler 7, the waste heat recovery boiler 7 is not communicated with the waste heat recovery boiler 7, the superheated steam outlet of the superheater 7 is communicated with the superheated steam inlet of the fluidized bed distillation chamber 3, the flue gas outlet of the superheater 7 is communicated with the flue gas inlet of the high-temperature air preheater 8, the flue gas outlet of the high-temperature air preheater 8 is communicated with the flue gas inlet of the economizer 9, the high-temperature air outlet of the high-temperature air preheater 8 is respectively communicated with the air chamber 11 at the bottom of the circulating fluidized bed 4 and the secondary air inlet 12 of the circulating fluidized bed 4 through a high-temperature air conveying pipeline, the flue gas outlet of the economizer 9 is communicated with the flue gas inlet of the low-temperature air preheater 10, the flue gas outlet of the low-temperature air preheater 10 is communicated with the flue gas inlet of the bag-type dust collector 19, the flue gas outlet of the bag-type dust collector 19 is communicated with the ash bin 20, the flue gas outlet of the bag-type dust collector 19 is communicated with the inlet of the fan 21, the lower part of the circulating fluidized bed 4 is provided with the discharge opening 22, and the discharge opening 22 is communicated with the slag inlet of the drum slag cooler 18 (discharging slag through the drum slag cooler 18).
The specific structure of the fluidized bed distillation chamber 3 in the present embodiment has been disclosed in the invention patent "a gasification, distillation reaction apparatus" (zl 201210395220. X); the specific structure of the multistage dryer 24 is disclosed in the invention patent "sludge multistage dryer, fluidized bed incineration disposal device and method" (zl 201210065531. X).
The beneficial effects of the embodiment are as follows:
1. the high-temperature ash of the circulating fluidized bed 4 is used as a heat source for distilling the oil sludge, the differential internal circulating fluidized bed distillation chamber is used as oil sludge distillation equipment, high-temperature steam is used as a fluidizing medium, the oil sludge and the high-temperature ash are fully mixed, the distillation effect of the oil sludge is good, and the evaporation rate of the oil in the oil sludge reaches over 90 percent.
2. The high-temperature fraction generated by the distillation of the oil sludge and the high-temperature steam are used as heat sources of the multistage dryer 24, so that the heat of the oil sludge distillation product is fully utilized, and the energy consumption is reduced.
3. The residue of the distillation of the oil sludge is sent into the circulating fluidized bed 4 for combustion, and the heat of the residue is utilized to realize the complete harmless treatment of the oil sludge.
The second embodiment is as follows: as shown in fig. 1, a method for recovering oil by distillation of sludge in a circulating fluidized bed by using the apparatus according to the first embodiment comprises the following steps:
the method comprises the following steps: sending the wet oil sludge with the water content of 70-80 percent after mechanical dehydration into a multistage dryer 24 by using an oil sludge pump 1 to dry the water content to 35-45 percent;
step two: the dried oil sludge enters an oil sludge groove 25, then the dried oil sludge is fed into a fluidized bed distillation chamber 3 for distillation by using an oil sludge plunger pump 26, distillation residues are fed into a circulating fluidized bed 4 for combustion, high-temperature flue gas generated by combustion in the circulating fluidized bed 4 carries high-temperature ash and firstly enters a primary cyclone separator 5, the high-temperature ash separated by the primary cyclone separator 5 is used as a distillation heat source and is fed into the fluidized bed distillation chamber 3, meanwhile, superheated steam with the temperature of 400-500 ℃ generated by a superheater 7 is fed into the fluidized bed distillation chamber 3 as a fluidizing medium, and the temperature in the fluidized bed distillation chamber 3 is 500-600 ℃;
step three: high-temperature fractions and steam which are generated by distillation of oil sludge and have the temperature of 500-600 ℃ are dedusted by the secondary cyclone separator 14, the high-temperature fractions and the steam enter the multistage dryer 24 to be used as heat sources for drying the oil sludge, the fractions and the steam which leave the multistage dryer 24 enter the condenser 15 to be condensed to obtain an oil-water mixture and uncondensed combustible gas, the oil-water mixture enters the oil-water separation system 16 to be separated to obtain oil, and the uncondensed combustible gas is fed into the circulating fluidized bed 4 through the uncondensed gas inlet 13 of the circulating fluidized bed 4 to be combusted;
step four: the non-condensable combustible gas in the circulating fluidized bed 4 and high-temperature flue gas generated by combustion of oil sludge distillation residues carry high-temperature ash to enter a primary cyclone separator 5, the high-temperature ash separated by the primary cyclone separator 5 directly enters a fluidized bed distillation chamber 3 to serve as a heating source of oil sludge, the high-temperature flue gas leaving the primary cyclone separator 5 and having the temperature of 850-900 ℃ firstly enters a waste heat boiler 6 to generate low-pressure saturated steam (the pressure is 0.3-0.5 MPa), and then the flue gas enters a superheater 7 and heats the low-pressure saturated steam generated in the waste heat boiler 6 to superheated steam of 400-500 ℃;
step five: the hot flue gas leaving the superheater 7 and having the temperature of 600-650 ℃ is subjected to heat exchange and temperature reduction sequentially through a high-temperature air preheater 8, an economizer 9 and a low-temperature air preheater 10, then enters a bag-type dust remover 19 to remove smoke dust, then reaches the standard and is discharged, the smoke dust separated by the bag-type dust remover 19 enters an ash bin 20, and meanwhile, the high-temperature air leaving the high-temperature air preheater 8 and having the temperature of 450-550 ℃ enters the circulating fluidized bed 4 through an air chamber 11 at the bottom of the circulating fluidized bed 4 and a secondary air inlet 12 on the side wall of the circulating fluidized bed 4 respectively to provide air required by combustion.
The beneficial effects of the embodiment are as follows:
1. the high-temperature ash of the circulating fluidized bed 4 is used as a heat source for distilling the oil sludge, the differential internal circulating fluidized bed distillation chamber is used as oil sludge distillation equipment, high-temperature steam is used as a fluidizing medium, the oil sludge and the high-temperature ash are fully mixed, the distillation effect of the oil sludge is good, and the evaporation rate of the oil in the oil sludge reaches over 90 percent.
2. The high-temperature fraction generated by the distillation of the oil sludge and the high-temperature steam are used as heat sources of the multistage dryer 24, so that the heat of the oil sludge distillation product is fully utilized, and the energy consumption is reduced.
3. The residue of the distillation of the oil sludge is sent into the circulating fluidized bed 4 for combustion, and the heat of the residue is utilized to realize the complete harmless treatment of the oil sludge.
The third concrete implementation mode: as shown in fig. 1, in the method for recovering oil by distillation of sludge in a circulating fluidized bed according to the second embodiment, in the fourth step, if the temperature of combustible gas that does not condense in the circulating fluidized bed 4 and high-temperature flue gas generated by combustion of sludge distillation residues does not reach 850-900 ℃, the partially dried sludge is added to the circulating fluidized bed 4, or coal is added to the circulating fluidized bed 4 to support combustion.
The fourth concrete implementation mode is as follows: as shown in fig. 2, a device for recovering oil by distillation of oil sludge in a circulating fluidized bed comprises a primary oil sludge pump 1A, a secondary oil sludge pump 1B, a fluidized bed distillation chamber 3, a circulating fluidized bed 4, a primary cyclone separator 5, a waste heat boiler 6, a superheater 7, a high-temperature air preheater 8, an economizer 9, a low-temperature air preheater 10, an air chamber 11, a secondary air inlet 12, a non-condensable gas (combustible gas) inlet 13, a secondary cyclone separator 14, a condenser 15, an oil-water separation system 16, an oil sludge or coal inlet 17, a roller slag cooler 18, a bag-type dust collector 19, an ash bin 20, an induced draft fan 21, a spiral feeder 23, a multi-stage dryer 24, a blade dryer 27, an oil sludge bin 2 and a discharge port 22, wherein the fluidized bed distillation chamber 3 is a differential internal circulation distillation chamber;
an outlet of the primary oil-sludge pump 1A is communicated with an oil sludge inlet of a multi-stage dryer 24, an inlet of the secondary oil-sludge pump 1B is communicated with an oil sludge outlet of the multi-stage dryer 24, an outlet of the secondary oil-sludge pump 1B is communicated with an oil sludge inlet of a paddle dryer 27, an oil sludge outlet of the paddle dryer 27 is communicated with an inlet of an oil sludge bin 2, an outlet of the oil sludge bin 2 is respectively communicated with an inlet of a screw feeder 23 and one end of a dry oil-sludge conveying pipeline, the other end of the dry oil-sludge conveying pipeline is arranged above an oil sludge or coal inlet 17 of a circulating fluidized bed 4, an outlet of the screw feeder 23 is communicated with an oil sludge inlet of the fluidized bed distillation chamber 3, a flue gas outlet of the circulating fluidized bed 4 is communicated with a flue gas inlet of a primary cyclone separator 5, an ash discharge port at the lower end of the primary cyclone separator 5 is communicated with a high-temperature ash inlet of the fluidized bed distillation chamber 3, a flue gas outlet of the primary cyclone separator 5 is communicated with a flue gas inlet of a waste heat superheater of the waste heat boiler 6, a flue gas outlet of the waste heat boiler 6 is communicated with a saturated steam outlet of the cyclone separator 7 and a saturated steam outlet of the steam distillation chamber 14, and a superheated steam outlet of the superheated steam separation chamber 14 are communicated with a superheated steam separation chamber 14, and a superheated steam separation chamber 14, the superheated steam separator 14; the distillation residue export of fluidized bed distillation chamber 3 and the distillation residue import intercommunication of circulating fluidized bed 4, the fraction and the steam export of multistage dryer 24 and two fractions of condenser 15 and one of them fraction and the steam import intercommunication of steam import, the fraction and the steam export of paddle dryer 27 and two fractions of condenser 15 and another fraction and the steam import intercommunication of steam import, the oil-water mixture export of condenser 15 and oil-water separation system 16's oil-water mixture import intercommunication, the noncondensable gas export of condenser 15 is through noncondensable gas conveying line and circulating fluidized bed 4's noncondensable gas (combustible gas) import 13 intercommunication, the exhansted gas outlet of superheater 7 and high temperature air heater 8's flue gas inlet intercommunication, high temperature air heater 8's flue gas outlet and economizer 9's flue gas inlet intercommunication, high temperature air heater 8's high temperature air outlet passes through high temperature air conveying line respectively with circulating fluidized bed 4 bottom's plenum 11 and circulating fluidized bed 4's overgrate air import 12 intercommunication, economizer 9's flue gas outlet and low temperature air heater 10's flue gas inlet intercommunication, low temperature air heater's bag dust collector's 19 and circulating fluidized bed 4's flue gas outlet 19, flue gas inlet intercommunication. The lower part of the circulating fluidized bed 4 is provided with a discharge opening 22, and the discharge opening 22 is communicated with a slag inlet of the roller slag cooler 18 (the slag is discharged through the roller slag cooler 18).
The specific structure of the fluidized-bed distillation chamber 3 in the present embodiment has been disclosed in the invention patent "a gasification, distillation reaction apparatus" (zl 201210395220. X); the specific structure of the multistage dryer 24 is disclosed in the invention patent "sludge multistage dryer, fluidized bed incineration treatment device and method" (zl201210065531. X).
The beneficial effects of the embodiment are as follows:
1. the high-temperature ash of the circulating fluidized bed 4 is used as a heat source for distilling the oil sludge, the differential internal circulating fluidized bed distillation chamber is used as oil sludge distillation equipment, high-temperature steam is used as a fluidizing medium, the oil sludge and the high-temperature ash are fully mixed, the distillation effect of the oil sludge is good, and the evaporation rate of the oil in the oil sludge reaches over 90 percent.
2. High-temperature fractions and high-temperature steam generated by oil sludge distillation are used as heat sources of the multistage dryer 24, so that the heat of oil sludge distillation products is fully utilized, and the energy consumption is reduced; and the oil sludge is further dehydrated by adopting the paddle dryer 27, so that the subsequent oil sludge conveying is simplified, and meanwhile, the temperature of the distillation chamber is increased, and the oil evaporation rate is improved.
3. The residue of the distillation of the oil sludge is sent into the circulating fluidized bed 4 for combustion, and the heat of the residue is utilized to realize the complete harmless treatment of the oil sludge.
The fifth concrete implementation mode is as follows: as shown in fig. 2, a method for recovering oil by distillation of sludge in a circulating fluidized bed by using the device according to the fourth embodiment comprises the following steps:
the method comprises the following steps: sending the wet oil sludge with the water content of 70-80% after mechanical dehydration into a multistage dryer 24 by using a first-stage oil sludge pump 1A to dry the water content to 35-45%;
step two: the dried oil sludge is sent into a blade dryer 27 by a secondary oil sludge pump 1B to continuously dry the water to 10-15%, and the dried oil sludge particles enter an oil sludge bin 2; then, the dried oil sludge is fed into a fluidized bed distillation chamber 3 by using a screw feeder 23 for distillation, high-temperature flue gas generated by combustion in a circulating fluidized bed 4 carries high-temperature ash and firstly enters a primary cyclone separator 5, the high-temperature ash separated by the primary cyclone separator 5 is taken as a distillation heat source and is fed into the fluidized bed distillation chamber 3, superheated steam with the temperature of 400-500 ℃ generated by a superheater 7 is taken as a fluidizing medium and is fed into the fluidized bed distillation chamber 3, and the temperature in the fluidized bed distillation chamber 3 is 500-600 ℃. The residue left after distillation is sent into the circulating fluidized bed 4 for combustion;
step three: high-temperature fractions and steam which are generated by distillation of oil sludge and have the temperature of 500-600 ℃ are dedusted by the secondary cyclone separator 14, the high-temperature fractions and the steam enter the multistage dryer 24 to be used as heat sources for drying the oil sludge, the fractions and the steam which leave the multistage dryer 24 and the paddle dryer 27 enter the condenser 15 to be condensed to obtain an oil-water mixture and uncondensed combustible gas, the oil-water mixture enters the oil-water separation system 16 to be separated to obtain oil, and the uncondensed combustible gas is fed into the circulating fluidized bed 4 through the uncondensed gas inlet 13 of the circulating fluidized bed 4 to be combusted;
step four: the non-condensable combustible gas in the circulating fluidized bed 4 and high-temperature flue gas generated by combustion of oil sludge distillation residues carry high-temperature ash to enter a primary cyclone separator 5, the high-temperature ash separated by the primary cyclone separator 5 directly enters a fluidized bed distillation chamber 3 to serve as a heating source of oil sludge, the high-temperature flue gas leaving the primary cyclone separator 5 and having the temperature of 850-900 ℃ firstly enters a waste heat boiler 6 to generate low-pressure saturated steam (the pressure is 0.6-1.0 MPa), part of the low-pressure saturated steam generated in the waste heat boiler 6 is sent into a paddle dryer 27 to be used for drying the oil sludge, the rest part of the low-pressure saturated steam enters a superheater 7, and the low-pressure saturated steam entering the superheater 7 is heated to 400-500 ℃ by utilizing the flue gas to serve as a fluidizing medium of the fluidized bed distillation chamber 3;
step five: the hot flue gas leaving the superheater 7 and having the temperature of 600-650 ℃ is subjected to heat exchange and temperature reduction sequentially through a high-temperature air preheater 8, an economizer 9 and a low-temperature air preheater 10, then enters a bag-type dust remover 19 to remove smoke dust, then reaches the standard and is discharged, the smoke dust separated by the bag-type dust remover 19 enters an ash bin 20, and meanwhile, the high-temperature air leaving the high-temperature air preheater 8 and having the temperature of 450-550 ℃ enters the circulating fluidized bed 4 through an air chamber 11 at the bottom of the circulating fluidized bed 4 and a secondary air inlet 12 on the side wall of the circulating fluidized bed 4 respectively to provide air required by combustion.
The beneficial effects of this embodiment are the same as those of the fifth embodiment.
The sixth specific implementation mode is as follows: as shown in fig. 2, in the method for recovering oil by distillation from sludge in a circulating fluidized bed according to the fifth embodiment, in the fourth step, if the temperature of combustible gas that does not condense in the circulating fluidized bed 4 and high-temperature flue gas generated by combustion of distillation residues of sludge does not reach 850 to 900 ℃, the partially dried sludge is added to the circulating fluidized bed 4, or coal is added to the circulating fluidized bed 4 to assist combustion.
Claims (6)
1. A device for recovering oil by circulating fluidized bed oil sludge distillation is characterized in that: the device comprises a sludge pump (1), a fluidized bed distillation chamber (3), a circulating fluidized bed (4), a primary cyclone separator (5), a waste heat boiler (6), a superheater (7), a high-temperature air preheater (8), an economizer (9), a low-temperature air preheater (10), an air chamber (11), a secondary air inlet (12), a non-condensable gas inlet (13), a secondary cyclone separator (14), a condenser (15), an oil-water separation system (16), a sludge or coal inlet (17), a roller slag cooler (18), a bag-type dust remover (19), an ash bin (20), a draught fan (21), a multistage dryer (24), a sludge tank (25), a sludge plunger pump (26) and a discharge opening (22), wherein the fluidized bed distillation chamber (3) is a differential internal circulating fluidized bed distillation chamber;
the export of oil sludge pump (1) and multistage dryer (24) the fatlute import intercommunication, multistage dryer (24) the fatlute export and fatlute groove (25) import intercommunication, the fatlute import of fatlute plunger pump (26) and the fatlute export intercommunication of fatlute groove (25), the fatlute export of fatlute plunger pump (26) respectively with the fatlute import and the fatlute conveying line intercommunication of fluidized bed distillation chamber (3), the export setting of fatlute conveying line in circulating fluidized bed (4) the top of fatlute or coal import (17), the import intercommunication of fluidized bed distillation chamber (3) high temperature fraction and vapor export and second grade cyclone (14), the device is characterized in that an outlet of the secondary cyclone separator (14) is communicated with a fraction and steam inlet of the multistage dryer (24), an ash discharge port is formed in the lower end of the secondary cyclone separator (14), a residue outlet of the fluidized bed distillation chamber (3) is communicated with a residue inlet of the circulating fluidized bed (4), a fraction and steam outlet of the multistage dryer (24) is communicated with a fraction and steam inlet of the condenser (15), an oil-water mixture outlet of the condenser (15) is communicated with an oil-water mixture inlet of the oil-water separation system (16), a non-condensable gas outlet of the condenser (15) is communicated with a non-condensable gas inlet (13) of the circulating fluidized bed (4) through a non-condensable gas conveying pipeline, and a flue gas outlet of the circulating fluidized bed (4) is communicated with a flue gas inlet of the primary cyclone separator (5) The system comprises a primary cyclone separator (5), an ash discharge port at the lower end of the primary cyclone separator (5) is communicated with a high-temperature ash inlet of a fluidized bed distillation chamber (3), a smoke outlet of the primary cyclone separator (5) is communicated with a smoke inlet of a waste heat boiler (6), a smoke outlet of the waste heat boiler (6) is communicated with a smoke inlet of a superheater (7), a saturated steam outlet of the waste heat boiler (6) is communicated with a saturated steam inlet of the superheater (7), an superheated steam outlet of the superheater (7) is communicated with a steam inlet of the fluidized bed distillation chamber (3), a smoke outlet of the superheater (7) is communicated with a smoke inlet of a high-temperature air preheater (8), a smoke outlet of the high-temperature air preheater (8) is communicated with a smoke inlet of an economizer (9), a high-temperature air outlet of the high-temperature air preheater (8) is communicated with an air chamber (11) at the bottom of the fluidized bed circulation (4) and a secondary air inlet (12) of the circulation fluidized bed (4) through a high-temperature air conveying pipeline, the smoke outlet of the economizer (9) is communicated with a low-temperature air preheater (10), a low-temperature air bag dust collector (19) is communicated with a smoke outlet of a smoke inlet (19) of a smoke inlet of a smoke bag dust inlet (19) and a draught fan (19), the lower part of the circulating fluidized bed (4) is provided with a discharge opening (22), and the discharge opening (22) is communicated with a slag inlet of the roller slag cooler (18).
2. A method for recovering oil by distillation of sludge in a circulating fluidized bed using the apparatus of claim 1, wherein: the method comprises the following steps:
the method comprises the following steps: sending the wet oil sludge with the water content of 70-80 percent after mechanical dehydration into a multistage dryer (24) by using an oil sludge pump (1) to dry the water content to 35-45 percent;
step two: the dried oil sludge enters an oil sludge groove (25), then the dried oil sludge is sent into a fluidized bed distillation chamber (3) for distillation by using an oil sludge plunger pump (26), distillation residues are sent into a circulating fluidized bed (4) for combustion, high-temperature smoke gas generated by combustion in the circulating fluidized bed (4) carries high-temperature ash to enter a primary cyclone separator (5) first, the high-temperature ash separated by the primary cyclone separator (5) is used as a distillation heat source to be sent into the fluidized bed distillation chamber (3), meanwhile, superheated steam with the temperature of 400-500 ℃ generated by a superheater (7) is used as a fluidizing medium to be sent into the fluidized bed distillation chamber (3), and the temperature in the fluidized bed distillation chamber (3) is 500-600 ℃;
step three: high-temperature fractions and steam which are generated by distillation of oil sludge and have the temperature of 500-600 ℃ are dedusted by a secondary cyclone separator (14), the high-temperature fractions and the steam enter a multistage dryer (24) to be used as heat sources to dry the oil sludge, the fractions and the steam which leave the multistage dryer (24) enter a condenser (15) to be condensed to obtain an oil-water mixture and uncondensed combustible gas, the oil-water mixture enters an oil-water separation system (16) to be separated to obtain oil, and the uncondensed combustible gas is fed into a circulating fluidized bed (4) through an uncondensed gas inlet (13) of the circulating fluidized bed (4) to be burnt;
step four: the method comprises the following steps that non-condensable combustible gas in a circulating fluidized bed (4) and high-temperature flue gas generated by combustion of oil sludge distillation residues carry high-temperature ash to enter a primary cyclone separator (5), the high-temperature ash separated by the primary cyclone separator (5) directly enters a fluidized bed distillation chamber (3) to serve as a heating source of oil sludge, the high-temperature flue gas leaving the primary cyclone separator (5) and having the temperature of 850-900 ℃ first enters a waste heat boiler (6) to generate low-pressure saturated steam, and then the flue gas enters a superheater (7) and heats the low-pressure saturated steam generated in the waste heat boiler (6) to superheated steam of 400-500 ℃;
step five: the hot flue gas leaving the superheater (7) and having the temperature of 600-650 ℃ sequentially passes through the high-temperature air preheater (8), the economizer (9) and the low-temperature air preheater (10) for heat exchange and temperature reduction, enters the bag-type dust remover (19) for smoke dust removal and then reaches the standard for emission, the smoke dust separated by the bag-type dust remover (19) enters the ash bin (20), and meanwhile, the high-temperature air leaving the high-temperature air preheater (8) and having the temperature of 450-550 ℃ enters the circulating fluidized bed (4) through the air chamber (11) at the bottom of the circulating fluidized bed (4) and the secondary air inlet (12) on the side wall of the circulating fluidized bed (4) respectively to provide air required for combustion.
3. The method of circulating fluidized bed sludge distillation for oil recovery of claim 2, wherein: in the fourth step of the method, the first step of the method,
and if the temperature of the non-condensable combustible gas in the circulating fluidized bed (4) and the high-temperature flue gas generated by the combustion of the oil sludge distillation residues does not reach 850-900 ℃, adding part of dried oil sludge into the circulating fluidized bed (4) or adding coal into the circulating fluidized bed (4) to support combustion.
4. A device for recovering oil by circulating fluidized bed oil sludge distillation is characterized in that: the device comprises a primary oil sludge pump (1A), a secondary oil sludge pump (1B), a fluidized bed distillation chamber (3), a circulating fluidized bed (4), a primary cyclone separator (5), a waste heat boiler (6), a superheater (7), a high-temperature air preheater (8), an economizer (9), a low-temperature air preheater (10), an air chamber (11), a secondary air inlet (12), a non-condensable gas inlet (13), a secondary cyclone separator (14), a condenser (15), an oil-water separation system (16), an oil sludge or coal inlet (17), a roller slag cooler (18), a cloth bag dust collector (19), an ash bin (20), an induced draft fan (21), a spiral feeder (23), a multi-stage dryer (24), a paddle dryer (27), an oil sludge bin (2) and a discharge port (22), wherein the fluidized bed distillation chamber (3) is a differential internal circulating fluidized bed distillation chamber;
the outlet of the primary oil sludge pump (1A) is communicated with an oil sludge inlet of a multistage dryer (24), the inlet of the secondary oil sludge pump (1B) is communicated with an oil sludge outlet of the multistage dryer (24), the outlet of the secondary oil sludge pump (1B) is communicated with an oil sludge inlet of a paddle dryer (27), an oil sludge outlet of the paddle dryer (27) is communicated with an inlet of an oil sludge bin (2), the outlet of the oil sludge bin (2) is respectively communicated with the inlet of a screw feeder (23) and one end of a dry oil sludge conveying pipeline, the other end of the dry oil sludge conveying pipeline is arranged above oil sludge or coal inlet (17) of a circulating fluidized bed (4), the outlet of the screw feeder (23) is communicated with an oil sludge inlet of a fluidized bed distillation chamber (3), the flue gas outlet of the circulating fluidized bed (4) is communicated with a flue gas inlet of a primary cyclone separator (5), a flue gas outlet at the lower end of the primary cyclone separator (5) is communicated with a high-temperature distillation chamber (3), the flue gas outlet of the primary cyclone separator (5) is communicated with a flue gas inlet of a steam superheater (7), and a flue gas inlet of a waste heat steam drying boiler (6) are respectively communicated with a flue gas superheater (7), the superheated steam outlet of the superheater (7) is communicated with the superheated steam inlet of the fluidized bed distillation chamber (3), the high-temperature fraction and steam outlet of the fluidized bed distillation chamber (3) is communicated with the inlet of a secondary cyclone separator (14), the outlet of the secondary cyclone separator (14) is communicated with the fraction and steam inlet of a multistage dryer (24), the lower end of the secondary cyclone separator (14) is provided with an ash discharge port, the distillation residue outlet of the fluidized bed distillation chamber (3) is communicated with the distillation residue inlet of the circulating fluidized bed (4), the fraction and steam outlet of the multistage dryer (24) is communicated with one of the two fractions of the condenser (15) and the steam inlet, the fraction and steam outlet of the paddle dryer (27) is communicated with the other of the two fractions of the condenser (15) and the steam inlet, the mixture outlet of the oil-water separator (16) is communicated with the oil-water mixture inlet of the superheater (16), the noncondensable steam outlet of the condenser (15) is communicated with the noncondensable air inlet of the circulating fluidized bed (4), the noncondensable air outlet of the high-temperature preheater (7) is communicated with the flue gas inlet of the circulating fluidized bed (8), and the flue gas outlet of the high-temperature preheater (8) of the circulating fluidized bed (4) are respectively communicated with the flue gas outlet of the flue gas preheater (8), and the flue gas outlet of the high-gas preheater (8), and the flue gas outlet of the high-gas preheater (8) of the high-temperature preheater (7), and the high-temperature preheater (8) of the high-temperature preheater (8) are respectively communicated with the high-temperature preheater, and the high-temperature preheater (11) And overfire air import (12) intercommunication of circulating fluidized bed (4), the exhanst gas outlet of economizer (9) and the exhanst gas inlet intercommunication of low temperature air heater (10), the exhanst gas outlet of low temperature air heater (10) and the exhanst gas inlet intercommunication of sack cleaner (19), the smoke and dust export and grey storehouse (20) intercommunication of sack cleaner (19), the exhanst gas outlet and draught fan (21) import intercommunication of sack cleaner (19), circulating fluidized bed (4) lower part is equipped with discharge opening (22), discharge opening (22) and the slag inlet intercommunication of cylinder cold sediment machine (18).
5. A method of recovering oil by distillation of sludge in a circulating fluidized bed using the apparatus of claim 4, wherein: the method comprises the following steps:
the method comprises the following steps: sending the wet oil sludge with the water content of 70-80 percent after mechanical dehydration into a multistage dryer (24) by using a first-stage oil sludge pump (1A) to dry the water content to 35-45 percent;
step two: the dried oil sludge is sent into a blade dryer (27) by a secondary oil sludge pump (1B) to continuously dry the water to 10-15%, and the dried oil sludge particles enter an oil sludge bin (2); then, the dried oil sludge is fed into a fluidized bed distillation chamber (3) by using a screw feeder (23) for distillation, high-temperature smoke gas generated by combustion in a circulating fluidized bed (4) carries high-temperature ash and firstly enters a primary cyclone separator (5), the high-temperature ash separated by the primary cyclone separator (5) is taken as a distillation heat source and is fed into the fluidized bed distillation chamber (3), meanwhile, superheated steam generated by a superheater (7) and having the temperature of 400-500 ℃ is taken as a fluidizing medium and is fed into the fluidized bed distillation chamber (3), the temperature in the fluidized bed distillation chamber (3) is 500-600 ℃, and the residual residues after distillation are fed into the circulating fluidized bed (4) for combustion;
step three: high-temperature fractions and steam which are generated by distillation of oil sludge and have the temperature of 500-600 ℃ are dedusted by a secondary cyclone separator (14), the oil sludge is dried by entering a multistage dryer (24) as a heat source, fractions and steam which leave the multistage dryer (24) and a blade dryer (27) enter a condenser (15) to be condensed to obtain an oil-water mixture and uncondensed combustible gas, the oil-water mixture enters an oil-water separation system (16) to be separated to obtain oil, and the uncondensed combustible gas is fed into a circulating fluidized bed (4) through an uncondensed gas inlet (13) of the circulating fluidized bed (4) to be combusted;
step four: the method comprises the following steps that non-condensable combustible gas in a circulating fluidized bed (4) and high-temperature flue gas generated by combustion of oil sludge distillation residues carry high-temperature ash to enter a primary cyclone separator (5), the high-temperature ash separated by the primary cyclone separator (5) directly enters a fluidized bed distillation chamber (3) to serve as a heating source of oil sludge, the high-temperature flue gas leaving the primary cyclone separator (5) and having the temperature of 850-900 ℃ firstly enters a waste heat boiler (6) to generate low-pressure saturated steam, one part of the low-pressure saturated steam generated in the waste heat boiler (6) is sent to a paddle dryer (27) to be used for drying the oil sludge, the rest part of the low-pressure saturated steam enters a superheater (7), and the low-pressure saturated steam entering the superheater (7) is heated to 400-500 ℃ by utilizing the flue gas to serve as a fluidizing medium of the fluidized bed distillation chamber (3);
step five: the hot flue gas leaving the superheater (7) and having the temperature of 600-650 ℃ sequentially passes through the high-temperature air preheater (8), the economizer (9) and the low-temperature air preheater (10) for heat exchange and temperature reduction, then enters the bag-type dust remover (19) for smoke dust removal, the smoke dust is discharged after reaching the standard, the smoke dust separated by the bag-type dust remover (19) enters the ash bin (20), and meanwhile, the high-temperature air leaving the high-temperature air preheater (8) and having the temperature of 450-550 ℃ respectively enters the circulating fluidized bed (4) through the air chamber (11) at the bottom of the circulating fluidized bed (4) and the secondary air inlet (12) on the side wall of the circulating fluidized bed (4) for providing air required for combustion.
6. The method of circulating fluidized bed sludge distillation for oil recovery of claim 5, wherein: in the fourth step of the method, the first step of the method,
and if the temperature of the non-condensable combustible gas in the circulating fluidized bed (4) and the high-temperature flue gas generated by the combustion of the oil sludge distillation residues does not reach 850-900 ℃, adding part of dried oil sludge into the circulating fluidized bed (4) or adding coal into the circulating fluidized bed (4) to support combustion.
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