CN112707610A - Process for resource utilization of oily sludge - Google Patents
Process for resource utilization of oily sludge Download PDFInfo
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- CN112707610A CN112707610A CN202011548835.2A CN202011548835A CN112707610A CN 112707610 A CN112707610 A CN 112707610A CN 202011548835 A CN202011548835 A CN 202011548835A CN 112707610 A CN112707610 A CN 112707610A
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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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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/10—Treatment of sludge; Devices therefor by pyrolysis
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- C—CHEMISTRY; METALLURGY
- 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
- C02F11/13—Treatment of sludge; Devices therefor by de-watering, drying or thickening by heating
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
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- 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
- F23G5/44—Details; Accessories
- F23G5/46—Recuperation of heat
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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
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
- F23G7/061—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating
- F23G7/065—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating using gaseous or liquid fuel
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2206/00—Waste heat recuperation
- F23G2206/20—Waste heat recuperation using the heat in association with another installation
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2209/00—Specific waste
- F23G2209/14—Gaseous waste or fumes
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/40—Valorisation of by-products of wastewater, sewage or sludge processing
Abstract
The invention relates to the technical field of oily sludge treatment, and discloses a process for resource utilization of oily sludge, which comprises the following treatment steps: crushing; 2) stirring and homogenizing; 3) dehydrating and removing light; 4) dry distillation; 5) pyrolyzing; 6) collecting and separating; 7) purifying; 8) and (4) recovering energy. According to the invention, by adopting the oily sludge pyrolysis treatment technology, the operation environment is friendly, the circular economy and good operation can be realized, and the application prospect is wide, but in the pyrolysis process in the prior art, the additive or the catalyst is added, so that the additive and the catalyst cannot be recycled, and solid wastes are increased.
Description
Technical Field
The invention relates to the technical field of oily sludge treatment, in particular to a process for resource utilization of oily sludge.
Background
The oily sludge is a viscous waste which is highly emulsified by oil, water and slag and is generated in the processes of oil exploitation, transportation, storage, tank cleaning and refining. Has the characteristics of complex components, toxicity, harm and difficult degradation. Contains a large amount of pathogenic bacteria, parasites (eggs), heavy metals such as copper, zinc, chromium, mercury and the like and other non-degradable toxic and harmful substances, and if the heavy metals and other non-degradable toxic and harmful substances are directly discharged without treatment, the heavy metals occupy a large amount of cultivated land, and pollute surrounding soil, water and air, thereby causing resource waste. According to the national records of hazardous waste (Ministry of Industrial waste No. 39, 2016, 8.1), oily sludge is classified as hazardous waste (HW08) by the nation and needs to be subjected to resource and harmless treatment. The oil content of the oil-containing sludge is 30-80%, and the method has great resource utilization potential.
The prior oily sludge resource utilization technology mainly comprises various methods such as sludge incineration, coking technology, solvent extraction technology, hot water washing treatment technology, sludge conditioning mechanical dehydration technology, ultrasonic deoiling technology, recharge profile control technology, surfactant elution technology, freeze thawing decrement technology, air floatation technology, electrochemical treatment technology and the like, wherein the following treatment technologies are the prior treatment technologies and one of the treatment technologies is simply explained as follows:
1. oily sludge incineration technology
The technology directly burns the oily sludge in a combustion furnace at high temperature, and has obvious reduction and thorough harmlessness. But the recoverable oil in the oily sludge is burnt, and dioxin is generated by combustion to cause secondary pollution.
2. Coking technology
The coking process technology for treating oil sludge is essentially deep heat treatment of heavy oil, and is a thermal conversion process of hydrocarbons, namely a high-temperature thermal cracking and thermal condensation process of the heavy oil. During thermal conversion, heavy oils typically begin cracking at around 370 ℃, while condensation reactions accelerate with increasing cracking severity. The coking technique requires the use of clay or the like as a coking catalyst. The clay mixed into the sludge cannot be recovered. Clay resources are limited.
3. Solvent extraction technology
Oily sludge is primarily a well emulsified mixture of oil, water and sludge. The extraction technology is that based on the principle of "similar and compatible" one kind of proper organic solvent is selected as extractant, and after the mixture is mixed with oil sludge and mass transfer occurs, oil is extracted from water into the extractant. Then, the extraction phase and the raffinate phase are layered with each other due to the density difference, so that the separation of oil-water-sludge three phases is realized, and the crude oil in the oil sludge is recycled. The solvent extraction technology can leave partial oil and solvent in the mud, the treatment is not thorough, the dosage of the extractant is large, and the use cost is high.
4. Oil sludge tempering-mechanical dewatering technology
The oil sludge is added with a conditioning agent, so that crude oil is separated from solid particles, oil drops are polymerized, and an originally added chemical agent is settled along with solid impurities, thereby realizing the separation of three phases of water, oil and slag. The oil content in the product slag of the technology is high, and the existence of chemical agents increases the share of waste.
5. Ultrasonic deoiling technology
The ultrasonic deoiling technology for oil sludge utilizes ultrasonic waves to destroy the structure of the oil sludge, reduces the viscosity of dirty oil in the sludge, reduces the adhesion effect of the dirty oil and the soil, and finally realizes demulsification so as to separate the dirty oil, water and the soil. The three-phase separation of the technology is not thorough, and other treatment technologies are required to be assisted.
6. Recharge profile control technology
The oil sludge is used as basic raw material, and because the oil sludge in the produced water has good compatibility with the stratum, a chemical treatment method is adopted, and a proper amount of chemical additives are added, so that not only can solid particles in the oil sludge be suspended, the suspension time be prolonged, the injection depth be increased, but also the plugging strength can be effectively improved, and the oil component can be uniformly dispersed to form stable and uniform emulsion. The technology is mainly used in the oil extraction process of the oil field, and can not treat a large amount of oily sludge.
7. Hot water washing treatment technology
The hot water washing treatment technology is mainly characterized in that oil sludge is added into hot water through a physical method, and some chemical additives such as surfactants are added to reduce the adhesive force between oil and sludge, so that the oil is desorbed from the solid phase surface or the separated sludge is aggregated to remove the oil. The oil sludge is washed, and process equipment such as stirring or air flotation is added to realize three-phase separation of oil, sludge and water. The oil sludge treated by the technology still contains a small amount of oil, is easy to generate secondary pollution, and needs to be additionally provided with wastewater treatment equipment. The running cost is high.
At present, the invention patent application with the patent number 201710030732.9 has the defect that the resource utilization cannot be realized.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides a process for resource utilization of oily sludge.
In order to solve the technical problem, the invention is solved by the following technical scheme:
a process for resource utilization of oily sludge comprises the following treatment steps:
1) crushing: the method comprises the following steps of (1) breaking and crushing the oily sludge and a packaging woven bag by using a double-shaft shredder, and crushing large materials such as metal plates, stones, glass, plastics, plate caking materials and the like in the oily sludge to form an oily sludge mixture;
2) stirring and homogenizing: stirring, homogenizing and homogenizing the crushed oil sludge mixture by a double-shaft homogenizing stirrer;
3) dewatering and removing light: carrying out radiation heat exchange on the homogenized and homogenized oil sludge mixture in a dehydration and light removal device, evaporating water and part of light components in the oil sludge mixture, and uniformly collecting the evaporated water and the light components;
4) dry distillation: conveying the dewatered and lightness-removed oil sludge mixture into a dry distillation device for dry distillation treatment to generate dry distillation gas, and uniformly collecting the dry distillation gas;
5) pyrolysis: conveying the oil sludge mixture subjected to dry distillation into a rotary pyrolysis furnace to form pyrolysis slag and pyrolysis gas, conveying part of high-temperature pyrolysis slag into a dry distillation device to be fully stirred and contacted with the oil sludge mixture subjected to dehydration and lightness removal, and heating for dry distillation;
6) collecting and separating: the dehydrated and lightened water and light components obtained in the step 3), the dry distillation gas obtained in the step 4) and the pyrolysis gas and the raised dust obtained in the step 5) form an oil-gas-water-vapor mixture together, the oil-gas-water-vapor-dust mixture is uniformly collected into a gas-solid separator through a pipeline, the separated gas is subjected to heat exchange through a heat exchanger and then enters a water cooler, the heat exchanger is a tubular heat exchanger, the tube pass is pyrolysis gas, the shell pass is air blown by a Roots blower, and finally the air enters a three-phase separator, fuel oil, sewage and non-condensable gas are obtained through separation of the three-phase separator and are respectively collected, the fuel oil is subjected to desulfurization treatment and can be sold outside a vehicle through an oil pump, the sewage is sent into a circulating water tower and a fire pool through a water pump, and the separated dust enters a pyrolysis residue buffer;
7) purifying: purifying the non-condensable gas obtained in the step 6) through flue gas alkali washing activated carbon adsorption treatment, heating the purified non-condensable gas and/or natural gas through a gas heat exchanger, and conveying the heated non-condensable gas and/or natural gas to a rotary pyrolysis furnace burner for burning and heating;
8) energy recovery: and (3) combusting the rotary pyrolysis furnace combustor in the step 5) to generate high-temperature flue gas, conveying the high-temperature flue gas into a gas heat exchanger, exchanging heat for the non-condensable gas and/or the natural gas in the step 7), conveying the high-temperature flue gas subjected to heat exchange and temperature reduction in the gas heat exchanger into a heat exchange tube nest of a dehydration and lightness-removing device through a pipeline for secondary heat exchange, and finally discharging the high-temperature flue gas after being processed to be qualified by a flue gas processing device.
Preferably, in step 5), the pyrolysis residue after carrying out the pyrolysis in the rotary pyrolysis furnace is sieved through the screening section of thick bamboo that sets up inside the pyrolysis furnace, the left side ejection of compact of pyrolysis residue powder cover shell and get into the transition feed bin, big lump material and metallic foreign matter glass stone etc. are followed ejection of compact cover shell right side ejection of compact and are gone into ejection of compact feed bin, still include hot-air transition jar and material seal pump, the hot-air in the hot-air transition jar is sent the pyrolysis residue powder to the transition feed bin through the material seal pump as the strength conveying source, there are two discharge gates below the transition feed bin, a discharge gate and dry distillation device intercommunication, another discharge gate and vertical cooling tower intercommunication further cool off the pyrolysis residue, the pyrolysis residue powder after the cooling forms the lime-ash.
Preferably, the ash is conveyed into an ash transition bin and then conveyed into a stock area through an FU chain conveyor, and the stock area is conveyed out for sale through an NE chain elevator, a bin top FU chain conveyor, an ash storage bin, a spiral gate at the bottom of the bin and a spiral conveyor and finally through a metering spiral truck.
Preferably, the cooling tower further comprises a Roots blower, and the Roots blower and the air distributor enter the bottom of the vertical cooling tower to cool ash after exchanging heat with the blast mixing heat exchanger.
Preferably, the system also comprises a first gas-solid separator and a second gas-solid separator, wherein the gas inlet of the first gas-solid separator is communicated with the transition bin, the solid discharge port of the first gas-solid separator is communicated with the vertical cooling tower, the gas inlet of the second gas-solid separator is communicated with the air distributor at the bottom of the vertical cooling tower and receives gas blown out by the Roots blower and the blown-in mixing heat exchanger, and the solid discharge port of the second gas-solid separator is connected with the ash transition bin; and gas discharge ports of the first gas-solid separator and the second gas-solid separator are communicated and convey gas to a hot air transition tank through a pipeline, and the hot air in the hot air transition tank is subjected to pressure regulation and is distributed to a rotary pyrolysis furnace and a material seal pump.
Preferably, the pyrolysis slag powder in the transition bin is conveyed to the dry distillation device through the conveying of the screw conveyor and is fully stirred, mixed and heated with the oil sludge mixture.
Preferably, the dry distillation device is a double-shaft stirring device, wherein the material inlet and the material outlet are provided with air-locking sealing valves, and the shell is provided with a heat exchange tube and a back mixing inlet.
Preferably, the rotary pyrolysis furnace is an indirect heating furnace, the material inlet and the material outlet are sealed by a metal expansion joint dynamic and static sealing ring, and the pressure of the dynamic and static sealing ring is adjusted by an air cylinder, so that the interior of the pyrolysis furnace is ensured to be in an anoxic state, the sealing of the sealing part is fully ensured, and the safe and efficient operation of the system is ensured; and collecting pyrolysis gas at the feed end of the pyrolysis furnace.
Preferably, in the step 1), the oil sludge packaging woven bag is lifted by an electric grab bucket and placed into a double-shaft shredder, and the crushed oily sludge material is transported to a double-shaft homogenizing mixer by a shaftless screw conveyor.
Preferably, in the step 2), the temperature of the flue gas of the tube nest in the double-shaft homogenizing mixer is 100-140 ℃, and in order to modify the acidity of the oil sludge, a calcium oxide additive is added into the double-shaft homogenizing mixer to be mixed together; in the step 3), the temperature of the flue gas of the heat exchange tube nest in the dehydration and lightness removal device is 260-300 ℃; in the step 4), the temperature of the flue gas of the heat exchange tube array of the dry distillation device is controlled to be 430-470 ℃; in the step 5), the temperature of the back-mixed pyrolysis slag is controlled to be 480-520 ℃, and the internal temperature of the rotary pyrolysis furnace is controlled to be 500-550 ℃; the temperature of the combustion chamber of the burner in the rotary pyrolysis furnace is 630-670 ℃.
Due to the adoption of the technical scheme, the invention has the remarkable technical effects that: according to the invention, by adopting the oil sludge pyrolysis treatment technology, the operation environment is friendly, the circular economy and good operation can be realized, and the application prospect is wide, but in the prior art, the additive or the catalyst is added in the pyrolysis process, the additive and the catalyst cannot be recycled, and the solid waste is increased.
Drawings
FIG. 1 is a process flow diagram of the present invention.
Fig. 2 is a diagram of the apparatus layout of the present invention.
Fig. 3 is a diagram of the apparatus of the present invention.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings and examples.
Example 1
A process for resource utilization of oily sludge comprises the following treatment steps as shown in the figure:
1) crushing: the method comprises the following steps of (1) breaking and crushing the oily sludge and a packaging woven bag by using a double-shaft shredder, and crushing large materials such as metal plates, stones, glass, plastics, plate caking materials and the like in the oily sludge to form an oily sludge mixture;
2) stirring and homogenizing: stirring, homogenizing and homogenizing the crushed oil sludge mixture by a double-shaft homogenizing stirrer;
3) dewatering and removing light: carrying out radiation heat exchange on the homogenized and homogenized oil sludge mixture in a dehydration and light removal device, evaporating water and part of light components in the oil sludge mixture, and uniformly collecting the evaporated water and the light components;
4) dry distillation: conveying the dewatered and lightness-removed oil sludge mixture into a dry distillation device for dry distillation treatment to generate dry distillation gas, and uniformly collecting the dry distillation gas;
5) pyrolysis: conveying the oil sludge mixture subjected to dry distillation into a rotary pyrolysis furnace for pyrolysis to form pyrolysis slag and pyrolysis gas, conveying part of high-temperature pyrolysis slag into a dry distillation device, fully stirring and contacting the high-temperature pyrolysis slag with the oil sludge mixture subjected to dehydration and lightness removal, and heating for dry distillation; and cooling the residual pyrolysis slag and then storing the cooled residual pyrolysis slag in a bin.
6) Collecting and separating: the dehydrated and lightness-removed water and light components obtained in the step 3), the dry distillation gas obtained in the step 4) and the pyrolysis gas and the dust obtained in the step 5) form an oil-gas-water-vapor dust mixture together, the oil-gas-water-vapor dust mixture is collected and enters a gas-solid separator through a pipeline, the separated gas enters a heat exchanger for heat exchange and then enters a water cooler, the heat exchanger is a tubular heat exchanger, the tube pass is pyrolysis gas, the shell pass is air blown by a Roots blower, the cooled matter finally enters a three-phase separator, fuel oil, sewage and non-condensable gas are obtained through the three-phase separator and collected respectively, the fuel oil is subjected to desulfurization treatment and can be sold outside a vehicle through an oil pump, the sewage is sent into a circulating water tower and a fire pool through a water pump, and the separated dust enters a pyrolysis slag buffer bin;
7) purifying: purifying the non-condensable gas obtained in the step 6) through flue gas alkali washing activated carbon adsorption treatment, heating the purified non-condensable gas and/or natural gas through a gas heat exchanger, and conveying the heated non-condensable gas and/or natural gas to a rotary pyrolysis furnace burner for combustion heating;
8) energy recovery: and (3) combusting the rotary pyrolysis furnace combustor in the step 5) to generate high-temperature flue gas, conveying the high-temperature flue gas into a gas heat exchanger, exchanging heat for the non-condensable gas and/or the natural gas in the step 7), conveying the high-temperature flue gas subjected to heat exchange and temperature reduction in the gas heat exchanger into a heat exchange tube nest of a dehydration and lightness-removing device through a pipeline for secondary heat exchange, and finally discharging the high-temperature flue gas after being processed to be qualified by a flue gas processing device.
Example 2
The same as embodiment 1, the difference is in step 5), the pyrolysis sediment after carrying out the pyrolysis in the gyration pyrolysis oven sieves through setting up at the inside screening section of thick bamboo of pyrolysis oven, the ejection of compact of pyrolysis sediment powder follow ejection of compact housing left side and get into the transition feed bin, lump material and metallic foreign matter glass stone etc. are followed ejection of compact housing right side ejection of compact and are gone into ejection of compact feed bin, still include hot-air transition jar and material seal pump, hot-air in the hot-air transition jar is sent the pyrolysis sediment powder to the transition feed bin through the material seal pump as the strength conveying source, there are two discharge gates below the transition feed bin, a discharge gate and dry distillation device intercommunication, another discharge gate and vertical cooling tower intercommunication and further cool off the pyrolysis sediment powder, the pyrolysis sediment powder after the cooling forms the lime-ash.
Conveying the ash slag to an ash slag transition bin, conveying the ash slag into a stock area through an FU chain conveyor, and finally carrying out outward transportation and sale through an NE chain elevator, a FU chain conveyor on the top of the stock, ash slag storage, a spiral gate at the bottom of the stock and a spiral conveyor in the stock area.
The vertical cooling tower also comprises a Roots blower, and the Roots blower and the air distributor at the bottom of the vertical cooling tower are used for cooling ash after the heat exchange of the Roots blower and the air entering the mixed heat exchanger.
The gas inlet of the first gas-solid separator is communicated with the transition bin, the solid discharge port of the first gas-solid separator is communicated with the vertical cooling tower, the gas inlet of the second gas-solid separator is communicated with the air distributor at the bottom of the vertical cooling tower and receives gas blown out by the Roots blower and the blown-in mixing heat exchanger, and the solid discharge port of the second gas-solid separator is connected with the ash transition bin; and gas discharge ports of the first gas-solid separator and the second gas-solid separator are communicated and convey gas to a hot air transition tank through a pipeline, and the hot air in the hot air transition tank is subjected to pressure regulation and is distributed to a rotary pyrolysis furnace and a material seal pump.
And conveying the pyrolysis slag powder in the transition bin into a dry distillation device through the conveying of a screw conveyor, and fully stirring, mixing and heating the pyrolysis slag powder with the oil sludge mixture.
The dry distillation device is a double-shaft stirring device with a gas locking seal at a material inlet and a material outlet and a heat exchange tube and a back mixing inlet at a shell.
The rotary pyrolysis furnace is an indirect heating furnace, the material inlet and the material outlet are sealed by a metal expansion joint dynamic and static sealing ring, and the pressure of the dynamic and static sealing ring is adjusted by an air cylinder, so that the interior of the pyrolysis furnace is ensured to be in an anoxic state, the sealing of the sealing part is fully ensured, and the safe and efficient operation of the system is ensured; and collecting pyrolysis gas at the feed end of the pyrolysis furnace.
In the step 1), the oil sludge packaging woven bag is lifted up through an electric grab bucket and placed into a double-shaft shredder, and the crushed oily sludge material is transported to a double-shaft homogenizing mixer through a shaftless screw conveyor.
Example 3
The same as the example 1, except that in the step 2), the temperature of flue gas of a shell tube of the double-shaft homogenizing mixer is 120 ℃, in order to modify the acidity of the oil sludge, the calcium oxide additive is added into the double-shaft homogenizing mixer to be mixed together; in the step 3), the temperature of the flue gas of the heat exchange tube array in the dehydration and lightness removal device is 280 ℃; in the step 4), the temperature of the flue gas of the heat exchange tube array of the dry distillation device is controlled at 450 ℃; in the step 5), the temperature of the back-mixed pyrolysis slag is controlled at 500 ℃, and the internal temperature of the rotary pyrolysis furnace is controlled at 530 ℃; the combustion chamber temperature of the burner in the rotary pyrolysis furnace was 650 ℃.
Claims (10)
1. A process for resource utilization of oily sludge is characterized by comprising the following steps: the method comprises the following processing steps:
1) crushing: the method comprises the following steps of (1) breaking and crushing the oily sludge and a packaging woven bag by using a double-shaft shredder, and crushing large materials such as metal plates, stones, glass, plastics, plate caking materials and the like in the oily sludge to form an oily sludge mixture;
2) stirring and homogenizing: stirring, homogenizing and homogenizing the crushed oil sludge mixture by a double-shaft homogenizing stirrer;
3) dewatering and removing light: carrying out radiation heat exchange on the homogenized and homogenized oil sludge mixture in a dehydration and light component removal device, evaporating water and light components in the oil sludge mixture, and uniformly collecting the evaporated water and light components;
4) dry distillation: conveying the dewatered and lightness-removed oil sludge mixture into a dry distillation device for dry distillation treatment to generate dry distillation gas, and uniformly collecting the dry distillation gas;
5) pyrolysis: conveying the oil sludge mixture subjected to dry distillation into a rotary pyrolysis furnace for pyrolysis to form pyrolysis slag and pyrolysis gas, conveying the high-temperature pyrolysis slag into a dry distillation device to be fully stirred and contacted with the oil sludge mixture subjected to dehydration and lightness removal, and heating for dry distillation;
6) collecting and separating: forming an oil-gas-water-vapor-dust mixture by the dehydrated and lightness-removed water and light components obtained in the step 3), the dry distillation gas obtained in the step 4) and the pyrolysis gas and dust obtained in the step 5) together, collecting the mixture into a gas-solid separator through a pipeline, performing heat exchange and cooling on the separated oil-gas-water-vapor, then feeding the cooled oil-gas-water-vapor into a three-phase separator, respectively obtaining fuel oil, sewage and non-condensable gas through the three-phase separator, and collecting the fuel oil, the sewage and the non-condensable gas respectively, and feeding the separated dust into a pyrolysis residue buffer bin;
7) purifying: purifying the non-condensable gas obtained in the step 6) through flue gas alkali washing activated carbon adsorption treatment, heating the purified non-condensable gas and/or natural gas through a gas heat exchanger, and conveying the heated non-condensable gas and/or natural gas to a burner in a rotary pyrolysis furnace for heating;
8) energy recovery: and (3) combusting the high-temperature flue gas generated by the combustor of the rotary pyrolysis furnace in the step 5) to generate high-temperature flue gas, conveying the high-temperature flue gas into the gas heat exchanger, exchanging heat for the non-condensable gas and/or the natural gas in the step 7), conveying the high-temperature flue gas subjected to heat exchange and temperature reduction in the gas heat exchanger into a heat exchange tube nest of the dehydration and lightness removal device through a pipeline for secondary heat exchange, and finally discharging the high-temperature flue gas after being processed to be qualified by the flue gas processing device.
2. The process for resource utilization of oily sludge according to claim 1, which is characterized in that: in step 5), the pyrolysis residue after the pyrolysis is carried out in the rotary pyrolysis furnace is sieved through a sieving barrel arranged inside the pyrolysis furnace, the pyrolysis residue powder enters a transition bin from the left side of a discharge housing, large lump materials, metal foreign matter glass stone blocks and the like are discharged from the right side of the discharge housing and enter the discharge bin, the rotary pyrolysis furnace further comprises a hot air transition tank and a material sealing pump, hot air in the hot air transition tank is used as a pneumatic conveying source to convey the pyrolysis residue powder to the transition bin through the material sealing pump, two discharge ports are arranged below the transition bin, one discharge port is communicated with a dry distillation device, the other discharge port is communicated with a vertical cooling tower and further cools the pyrolysis residue powder, and the cooled pyrolysis residue powder forms ash.
3. The process for resource utilization of oily sludge according to claim 2, which is characterized in that: conveying the ash slag to an ash slag transition bin, conveying the ash slag into a stock area through an FU chain conveyor, and finally carrying out outward transportation and sale through an NE chain elevator, a FU chain conveyor on the top of the stock, ash slag storage, a spiral gate at the bottom of the stock and a spiral conveyor in the stock area.
4. The process for resource utilization of oily sludge according to claim 2, which is characterized in that: the vertical cooling tower also comprises a Roots blower, and the Roots blower and the air distributor at the bottom of the vertical cooling tower are used for cooling ash after the heat exchange of the Roots blower and the air entering the mixed heat exchanger.
5. The process for resource utilization of oily sludge according to claim 4, which is characterized in that: the gas inlet of the first gas-solid separator is communicated with the transition bin, the solid discharge port of the first gas-solid separator is communicated with the vertical cooling tower, the gas inlet of the second gas-solid separator is communicated with the air distributor at the bottom of the vertical cooling tower and receives gas blown out by the Roots blower and the blown-in mixing heat exchanger, and the solid discharge port of the second gas-solid separator is connected with the ash transition bin; and gas discharge ports of the first gas-solid separator and the second gas-solid separator are communicated and convey gas to a hot air transition tank through a pipeline, and the hot air in the hot air transition tank is subjected to pressure regulation and is distributed to a rotary pyrolysis furnace and a material seal pump.
6. The process for resource utilization of oily sludge according to claim 2, which is characterized in that: and conveying the pyrolysis slag powder in the transition bin into a dry distillation device through the conveying of a screw conveyor, and fully stirring, mixing and heating the pyrolysis slag powder with the oil sludge mixture.
7. The process for resource utilization of oily sludge according to claim 1, which is characterized in that: the dry distillation device is a double-shaft stirring device with a material inlet and a material outlet provided with a gas locking seal valve, and a shell provided with a heat exchange tube and a back mixing inlet.
8. The process for resource utilization of oily sludge according to claim 1, which is characterized in that: the rotary pyrolysis furnace is an indirect heating furnace, the material inlet and the material outlet are sealed by a metal expansion joint dynamic and static sealing ring, and the dynamic and static sealing ring is subjected to pressure regulation by an air cylinder; and collecting pyrolysis gas at the feed end of the pyrolysis furnace.
9. The process for resource utilization of oily sludge according to claim 1, which is characterized in that: in the step 1), the oil sludge packaging woven bag is lifted up through an electric grab bucket and placed into a double-shaft shredder, and the crushed oily sludge material is transported to a double-shaft homogenizing mixer through a shaftless screw conveyor.
10. The process for resource utilization of oily sludge according to claim 1, which is characterized in that: in the step 2), the temperature of the flue gas of the tube nest in the double-shaft homogenizing mixer is 100-140 ℃, and a calcium oxide additive is added into the double-shaft homogenizing mixer to be mixed together; in the step 3), the temperature of the flue gas of the heat exchange tube nest in the dehydration and lightness removal device is 260-300 ℃; in the step 4), the temperature of the flue gas of the heat exchange tube array of the dry distillation device is controlled to be 430-470 ℃; in the step 5), the temperature of the back-mixed pyrolysis slag is controlled to be 480-520 ℃, and the internal temperature of the rotary pyrolysis furnace is controlled to be 500-550 ℃; the temperature of the combustion chamber of the burner in the rotary pyrolysis furnace is 630-670 ℃.
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