CN111153577A - Oily sludge treatment device and treatment method - Google Patents
Oily sludge treatment device and treatment method Download PDFInfo
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- CN111153577A CN111153577A CN202010069447.XA CN202010069447A CN111153577A CN 111153577 A CN111153577 A CN 111153577A CN 202010069447 A CN202010069447 A CN 202010069447A CN 111153577 A CN111153577 A CN 111153577A
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- 238000000034 method Methods 0.000 title claims abstract description 49
- 238000000197 pyrolysis Methods 0.000 claims abstract description 97
- 238000011084 recovery Methods 0.000 claims abstract description 90
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 31
- 230000023556 desulfurization Effects 0.000 claims abstract description 31
- 239000003921 oil Substances 0.000 claims description 87
- 239000007789 gas Substances 0.000 claims description 77
- 239000002918 waste heat Substances 0.000 claims description 40
- 239000010724 circulating oil Substances 0.000 claims description 31
- 239000007921 spray Substances 0.000 claims description 28
- 230000008569 process Effects 0.000 claims description 23
- 239000002912 waste gas Substances 0.000 claims description 23
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Classifications
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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
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
- C10K1/046—Reducing the tar content
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
- F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
- F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
-
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/40—Valorisation of by-products of wastewater, sewage or sludge processing
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- Environmental & Geological Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Water Supply & Treatment (AREA)
- Gasification And Melting Of Waste (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention provides an oily sludge treatment device, which is used for treating oily sludge and comprises a conveying unit, a pyrolysis unit, an oil recovery unit, a residue recovery unit, an incineration unit and a denitration and/or desulfurization unit. In addition, the invention also provides a treatment method of the oily sludge. The device and the method provided by the invention can effectively recover products such as oil, coke and the like from the oily sludge, realize the resource treatment of the oily sludge, have low operation cost and high discharge standard, and can be operated safely and stably for a long period.
Description
Technical Field
The invention relates to the field of sludge treatment, in particular to an oil-containing sludge treatment device and a treatment method.
Background
In petroleum exploitation, storage, processing, petrochemical industry, coal chemical industry and other production processes, oily sludge is generated, the oily sludge is a mixture of oil substances (high-boiling point organic compounds), water, dust particles and other impurities, at present, measures such as gravity settling, mechanical centrifugal separation and the like are generally adopted for concentration and decrement, part of oil is recovered, and residual residues are used as fuel for blending combustion or used as hazardous waste for incineration treatment.
In the process of coal gasification or coking, high-boiling-point organic compounds generated under high-temperature conditions are mixed with coal dust, solid particles and the like carried in coal gas during condensation to form coal tar residues, and the coal tar residues contain various substances such as benzene, phenols, naphthalene and the like, and also contain various organic compounds which have carcinogenic effects on organisms such as benzo (a) pyrene and the like, and have great harmfulness. Nevertheless, the coal tar residue has high heat value due to the fact that the coal tar residue contains a large amount of fixed carbon and organic volatile matters, and the ash content and the sulfur content are both low, so that the coal tar residue is a high-value secondary energy source if reasonably utilized. The common treatment method for the coal tar residue comprises solvent extraction, blending combustion, coal blending and the like, the investment and the operation cost of the solvent extraction are high, the operation is complex, and the blending combustion and the coal blending of the tar residue are not allowed along with the improvement of the national environmental protection requirement. Therefore, an oily sludge treatment system and method with reasonable investment and operation cost and stable and reliable operation are urgently needed.
Disclosure of Invention
In view of the above-mentioned need for oily sludge treatment and the drawbacks of the treatment techniques, it is an object of the present invention to provide an oily sludge treatment apparatus and a treatment method.
The invention provides an oily sludge treatment device, which is used for treating oily sludge and comprises: the conveying unit is used for storing and conveying the oily sludge; the pyrolysis unit is connected with the conveying unit and is used for carrying out pyrolysis treatment on the conveyed oily sludge; the oil recovery unit is connected with the pyrolysis unit and used for dedusting pyrolysis process gas generated by the pyrolysis unit and cooling and recovering oil in the pyrolysis process gas; the incineration unit is connected with the oil recovery unit and is used for carrying out incineration treatment on the waste gas subjected to dust removal and oil removal by the oil recovery unit; and the residue recovery unit is connected with the pyrolysis unit and used for cooling and recovering the solid residue generated by the pyrolysis unit.
According to an embodiment of the invention, the pyrolysis unit comprises an external thermal rotary furnace; preferably, the pyrolysis unit is connected with the waste heat recovery unit.
According to another embodiment of the invention, the oil recovery unit comprises a spray tower, an oil circulation spray system, a circulating oil filtration system and a circulating oil cooling system.
According to another embodiment of the present invention, the oil recovery unit further comprises a liquid separation system for separating liquid droplets entrained in the sprayed and deoiled exhaust gas.
According to another embodiment of the invention, the residue recovery unit comprises a slag cooler, an ash bucket and an ash bucket discharge valve, and the ash bucket level indicator opens and closes the discharge valve according to the level of the residue in the ash bucket.
According to another embodiment of the invention, the oily sludge treatment device further comprises a waste heat recovery unit, and the waste heat recovery unit is connected with the incineration unit and used for cooling the incineration tail gas of the incineration unit and recovering heat energy of the incineration tail gas.
According to another embodiment of the invention, the oily sludge treatment device further comprises an incineration tail gas denitration unit and/or desulfurization unit, wherein the incineration tail gas denitration and/or desulfurization unit is connected with the waste heat recovery unit and is used for carrying out denitration and/or desulfurization treatment on the tail gas of the waste heat recovery unit.
The invention also provides a treatment method of the oily sludge, which is used for treating the oily sludge and comprises the following steps: a conveying step of storing and conveying the oily sludge; a pyrolysis step of subjecting the oily sludge conveyed in the conveying step to pyrolysis treatment; an oil recovery step, wherein the pyrolysis process gas generated in the pyrolysis step is subjected to dust removal and is cooled to recover oil in the pyrolysis process gas; an incineration step, wherein the waste gas after dust and oil removal in the oil recovery step is incinerated; and a residue recovery step of cooling and recovering the solid residue generated in the pyrolysis step.
According to an embodiment of the present invention, the pyrolysis step is performed in an oxygen-free atmosphere, and the pyrolysis temperature is 200 to 800 ℃, preferably 300 to 750 ℃, and more preferably 400 to 700 ℃.
According to another embodiment of the present invention, the oil recovery step uses the recovered oil as a circulating spray medium for recycling, and filters and cools the circulating oil; preferably, the filtration precision is 5-100 microns.
According to another embodiment of the present invention, the temperature of both the gas and the circulating oil in the oil recovering step is higher than the boiling point of water; preferably 100 to 130 ℃.
According to another embodiment of the invention, the waste gas entering the incineration step from the oil recovery step is accompanied by heat.
According to another embodiment of the invention, the oily sludge treatment method further comprises a waste heat recovery step, wherein the incineration tail gas generated in the incineration step is subjected to cooling treatment; the temperature of the gas after waste heat recovery is 100-400 ℃, and more preferably 220-380 ℃.
According to another embodiment of the invention, the oily sludge treatment method further comprises a denitration and/or desulfurization step of the incineration exhaust gas, and the tail gas generated in the incineration exhaust gas waste heat recovery step is subjected to denitration and/or desulfurization treatment.
The device and the method provided by the invention can effectively recover products such as oil, coke and the like from the oily sludge, realize the resource treatment of the oily sludge, have low operation cost and high discharge standard of sludge treatment, and can be safely and stably operated for a long period.
Drawings
The above and other features and advantages of the present invention will become more apparent by describing in detail exemplary embodiments thereof with reference to the attached drawings.
FIG. 1 is a schematic view of an oily sludge treatment system of the present invention.
FIG. 2 is a flow chart of the method for treating oily sludge of the present invention.
Wherein the reference numerals are as follows:
1. a sludge conveying unit; 2. a pyrolysis unit; 3. an oil recovery unit; 4. an incineration unit; 5. a waste heat recovery unit; 6. a denitration unit; 7. a desulfurization unit; 8. a residue recovery unit; 9. a waste heat recovery unit;
A. sludge to be treated; B. a fuel gas; C. the pyrolysis furnace burns flue gas; D. pyrolyzing the residue; E. pyrolyzing the process gas; F. oily waste residues; G. recovering the oil; H. deoiling the waste gas; I. a denitration reducing agent; J. a desulfurizing agent; K. desulfurization waste water; l, exhaust gas; m, cooling to obtain solid residues; n, combustion air;
s1, a conveying step; s2, pyrolysis; s3, oil recovery; s4, burning; s5, a residue recovery step.
Detailed Description
To make the objects, technical solutions and advantages of the present invention clearer, example embodiments will now be described more fully with reference to the accompanying drawings. Example embodiments may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein; rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the concept of example embodiments to those skilled in the art. The same reference numerals in the drawings denote the same or similar structures, and thus their detailed description will be omitted.
The invention provides an oily sludge treatment device which can be used for treating oily sludge and comprises a sludge conveying unit 1, a pyrolysis unit 2, an oil recovery unit 3, an incineration unit 4 and a residue recovery unit 8 as shown in figure 1.
The sludge conveying unit 1 is used for storing and conveying the oily sludge A. Specifically, the oily sludge a firstly enters the sludge conveying unit 1, and the sludge conveying unit 1 is provided with a sludge storage tank and a sludge conveying pump for quantitatively conveying the sludge to the pyrolysis unit 2. The sludge storage tank and the sludge delivery pump are not particularly limited, and the sludge storage tank and the sludge delivery pump which are common in the field can be adopted, for example, a concrete or steel storage tank, a screw pump or a sludge screw conveyor and the like can be adopted, and the sludge can be quantitatively delivered to the pyrolysis unit.
And the pyrolysis unit 2 is connected with the sludge storage unit 1 and is used for carrying out pyrolysis treatment on the oily sludge conveyed from the sludge storage unit 1. The sludge of the sludge conveying unit 1 is conveyed to the pyrolysis unit 2, the pyrolysis unit 2 is provided with a pyrolysis furnace, the pyrolysis furnace is an external heating type rotary furnace, and the combustion of fuel and the pyrolysis of oil-containing sludge are respectively carried out in two independent spaces. The fuel gas B is adopted to burn and heat outside the rotary furnace body, the sludge enters the rotary furnace body, chemical reaction processes including vaporization, pyrolysis, dehydrogenation, thermal condensation, carbonization and the like are carried out under the oxygen-free, non-combustion and high-temperature states, the moisture in the oily sludge is evaporated, and organic matters are converted into water vapor, tar and coke.
In a preferred embodiment, the furnace temperature of the pyrolysis furnace may be 200 to 800 ℃, more preferably 300 to 750 ℃, and still more preferably 400 to 700 ℃, so as to evaporate all the water and oil in the oily sludge without adhering residual tar and dust or particles to the inner wall of the pyrolysis furnace, and if the oil and dust adhere to the inner wall of the pyrolysis furnace, the unloading of the residue and the long-term stable operation of the device are affected, of course, the lower operating temperature is beneficial to saving energy consumption and prolonging the service life of the equipment.
The pyrolysis furnace is not particularly limited, and an external heating type converter which is common in the field can be adopted, and the pyrolysis furnace is kept at positive pressure in order to keep an oxygen-free environment in the pyrolysis furnace. Moisture and oil (namely pyrolysis process gas E) gasified in the pyrolysis furnace by the sludge enter the subsequent oil recovery unit 3 under the action of positive pressure, pyrolysis residue D enters the residue recovery unit 8, and pyrolysis furnace combustion flue gas C formed by combustion of fuel gas B and air outside the pyrolysis furnace enters the waste heat recovery unit 9 for energy recovery and utilization. The waste heat recovery unit 9 comprises a pyrolysis furnace combustion smoke waste heat recoverer, and the heat in the combustion smoke of the high-temperature pyrolysis furnace is recycled to directly discharge low-temperature smoke. The waste heat recoverer is not particularly limited, and can adopt a waste heat boiler commonly used in the field to generate steam, and can also adopt a gas-gas heat exchanger to heat combustion-supporting air and the like.
And the oil recovery unit 3 is connected with the pyrolysis unit 2 and used for dedusting the pyrolysis process gas E generated by the pyrolysis unit 2 and cooling and recovering oil G in the pyrolysis process gas. The oil recovery unit 3 is provided with a spray tower, an oil circulation spray system, a spray circulation pump, a circulation oil filtration system and a circulation oil cooling system. And the pyrolysis process gas E enters the spray tower from the middle part of the spray tower and is in countercurrent contact with the circulating oil sprayed out from the spray system at the top of the spray tower, dust carried in the pyrolysis process gas E is leached out and enters the circulating oil collecting tank at the bottom, meanwhile, the temperature of the pyrolysis process gas E is reduced, and the oil in a gasification state is condensed out along with the reduction of the temperature and enters the circulating oil collecting tank. And the spraying circulating pump extracts circulating oil from the circulating oil collecting tank, dust and particles in the circulating oil are removed by filtering through a circulating oil filtering system, and the circulating oil is cooled by a circulating oil cooling system and then sent to a spraying system at the top of the tower for recycling. The condensed excessive oil (namely, recovered oil G) is discharged out of the oil recovery unit 3 according to the liquid level control of the circulating oil collecting tank, solid particles intercepted by the circulating oil filtering system are discharged out by oily residues F through backwashing, and the solid particles are sent to a sludge storage tank of the sludge conveying unit 1 for continuous treatment.
In order to prevent the moisture in the pyrolysis process gas from being condensed, the temperature of the process gas and the temperature of the circulating oil in the oil recovery unit are both higher than the boiling point of water, otherwise, the condensed water forms an emulsified state with oil and dust, and therefore the filtering system and the circulating spraying system are blocked. In a preferred embodiment, the temperature of the circulating oil is 100 to 130 ℃.
The spray tower of the present invention is not particularly limited, and for example, a spray tower commonly used in the art may be used, a packing layer may be provided or not provided in the spray tower, and the spray layer may be one or more layers. The invention is not particularly limited to the oil circulation spraying system, which may be a nozzle or a liquid distributor. The spraying circulating pump is not particularly limited, and can be a common centrifugal pump or other delivery pumps with the same function. The circulating oil filtering system is not particularly limited, a metal sintered filter or other filters can be used for the circulating oil filtering system, so long as the metal sintered filter or other filters can withstand the use temperature and the medium characteristics of the circulating oil, the filtering precision of the filter is not particularly limited, so long as the metal sintered filter or other filters can filter out most of particles in the circulating oil, and the use effect of the spraying system is not influenced. The circulating oil cooling system is not particularly limited, and a common shell-and-tube heat exchanger or other heat exchangers can be adopted, and the cooling medium can be water, air, oil or any other available medium. In order to separate the liquid oil drops in the gas phase as thoroughly as possible, the oil recovery unit 3 may also be provided with a liquid separation system at the rear end of the spray tower. The spray deoiling device is used for further separating liquid drops entrained in the waste gas after spray deoiling. The liquid separating system is not particularly limited, for example, a liquid separating tank and a wire mesh demister which are commonly used in the field can be used, and the liquid separating system can be arranged separately from the spray tower or can be designed into a whole with the spray tower.
And the incineration unit 4 is connected with the oil recovery unit 3 and is used for carrying out incineration treatment on the waste gas H subjected to dust removal and oil removal by the oil recovery unit 3. The deoiled exhaust gas H flowing out of the oil recovery unit 3 enters the incineration unit 4. The treatment device comprises an oil recovery unit 3 and an exhaust gas H which enters an incineration unit 4 to be accompanied by heat so as to prevent the temperature of the exhaust gas H from dropping to cause the condensation and the separation of gaseous oil substances. The invention has no special limitation on the heat tracing form, and can be any suitable heat tracing in the prior art to realize the purpose of preventing the temperature of the waste gas H from being reduced. The incineration unit 4 is provided with an incinerator in which the waste gas and combustion air N undergo a combustion oxidation reaction to combust the organic matter into CO2With water, sulfides to SO2Combustion of nitrogen-containing compounds to NOxAnd releases heat.
The incineration unit 4 may also be connected to a waste heat recovery unit 5. The waste heat recovery unit 5 is used for cooling the incineration tail gas of the incineration unit and recovering heat energy of the incineration tail gas. The waste gas after burning gets into waste heat recovery unit 5, and waste heat recovery unit 5 is provided with the waste heat recoverer, and the heat in the waste gas of waste heat recovery utilization makes the temperature of waste gas satisfy the temperature requirement of follow-up denitration unit. The waste heat recoverer is not particularly limited, and can adopt a waste heat boiler commonly used in the field to generate steam, and can also adopt a gas-gas heat exchanger to heat combustion-supporting air and the like.
The waste gas treated by the waste heat recovery unit 5 can also enter an incineration tail gas denitration unit 6 and/or a desulfurization unit 7 for carrying out denitration and/or desulfurization treatment on the tail gas of the waste heat recovery unit 5. The waste gas flowing out of the waste heat recovery unit 5 enters a denitration unit 6, the denitration unit 6 is provided with a denitration reactor, a denitration catalyst is filled in the denitration reactor, and NO in the waste gas is reacted by the denitration catalystxReacting with denitration reducer I to react NOxReduction to N2. The denitration reactor is not particularly limited, and an SCR denitration reactor commonly used in the field can be adopted. The denitration catalyst and the denitration reducing agent are not particularly limited, and the SCR low-temperature or high-temperature denitration catalyst and NH commonly used in the field can be adopted3And denitration reducing agents such as urea. The temperature of the denitration reaction is not particularly limited, and the reaction temperature is matched with the denitration catalyst, and in a preferred embodiment, the temperature of the denitration reaction is 200-400 ℃.
The waste gas flowing out of the denitration unit 6 enters a desulfurization unit 7, the desulfurization unit 7 is provided with a desulfurization tower and a desulfurization liquid circulating spray system, the waste gas is in countercurrent contact with desulfurization circulating liquid in the desulfurization tower, SO2 in the waste gas is absorbed into the desulfurization circulating liquid and reacts with a desulfurizer J added into the desulfurization circulating liquid to generate sulfite or sulfate, the desulfurized exhaust gas L is directly discharged, and the formed sulfite or sulfate is discharged outside desulfurization wastewater K. The desulfurization tower is not particularly limited, for example, the desulfurization tower commonly used in the field can be adopted, a packing layer can be arranged or not arranged in the desulfurization tower, the spraying layer can be one or more layers, the spraying system can be a nozzle or a liquid distributor, and the spraying circulating pump can be a commonly used centrifugal pump or other conveying pumps with the same function. The invention has no special limitation on the type of the desulfurizer,for example, lime, gypsum, NaOH, NH3Alkali desulfurizer can also be H2O2And the like, as long as the desulfurized exhaust gas meets the emission standard.
And a residue recovery unit 8 connected to the pyrolysis unit 4 for cooling and recovering the solid residue D generated from the pyrolysis unit 4. The residue recovery unit 8 is provided with a slag cooler, an ash bucket and a discharge valve. The pyrolysis residue D entering the residue recovery unit 8 is high in temperature, is cooled by the slag cooler and then enters the ash bucket, the ash bucket is provided with a material level meter, and the discharge valve is opened and closed according to the material level of the residue in the ash bucket, so that the proper material level is maintained in the ash bucket, and the pyrolysis process gas E in the pyrolysis furnace is prevented from escaping from the ash bucket. The slag cooler of the present invention is not particularly limited, and any slag cooler commonly used in the art may be used, and any cooling medium may be used, for example, circulating cooling water may be used.
The invention also provides a method for treating oily sludge, which is used for treating the oily sludge and comprises the following treatment steps with reference to the system shown in figure 1 and figure 2: a conveyance step (S1), a pyrolysis step (S2), an oil recovery step (S3), an incineration step (S4), and a residue recovery step (S5).
The oily sludge is stored and transported by the transporting step S1.
The oily sludge sent from the sending step is subjected to pyrolysis treatment by the pyrolysis step S2. In a preferred embodiment, in the pyrolysis step, the pyrolysis temperature is 200 to 800 ℃, preferably 300 to 750 ℃, and more preferably 400 to 700 ℃. So as to evaporate all the water and oil in the oily sludge without adhering residual tar and dust or particles to the inner wall of the equipment, thereby facilitating the long-term stable operation of the equipment.
The pyrolysis process gas generated in the pyrolysis step is dedusted and cooled to recover oil content in the pyrolysis process gas through an oil recovery step S3. In a preferred embodiment, the recovered oil is recycled as a circulating spray medium, and the circulating oil is filtered and cooled. Preferably, the filtration precision can be 5 to 100 micrometers. The temperature of gas and circulating oil in the oil recovery step is higher than the boiling point of water, so that the condensed water, oil and dust are prevented from forming an emulsified state, and a filtering system and a circulating spraying system are prevented from being blocked. Preferably, the temperature of the gas and the circulating oil in the step is 100-130 ℃.
In the incineration step S4, the exhaust gas after the oil recovery step is dedusted and deoiled is incinerated. In a preferred embodiment, the exhaust gas entering the incineration step S4 from the oil recovery step S3 is accompanied by heat to prevent the temperature of the gas entering the incineration plant from dropping. In a preferred embodiment, the exhaust gas after the incineration step S4 is subjected to a waste heat recovery step, and the incineration exhaust gas generated in the incineration step S4 is subjected to a temperature reduction treatment. The temperature of the gas after waste heat recovery is 100-400 ℃, and more preferably 220-380 ℃. In a preferred embodiment, the tail gas after waste heat recovery is subjected to a tail gas denitration and/or desulfurization step, and the tail gas generated in the tail gas waste heat recovery step is subjected to denitration and/or desulfurization treatment, so that the discharged tail gas reaches the emission standard.
The solid residue generated from the pyrolysis step is cooled and recovered through the residue recovery step S5.
The present invention will be described in further detail below with reference to examples.
Example 1
The oily sludge treatment was carried out according to the following procedure.
a. Oily sludge to be treated, containing water: 7%, oil 30%, sulfur 0.25%, N content 0.25%.
b. The oil-containing sludge is conveyed to a pyrolysis furnace by a screw pump, the pyrolysis furnace adopts an external heating type converter and is heated by burning natural gas, the temperature of the pyrolysis furnace is 700 ℃, the pressure in the furnace is 30Pa, the rotating speed of the converter is 3 r/min, and the retention time of the sludge in the pyrolysis furnace is 300 min.
c. The pyrolysis process gas enters an oil recovery spray tower, an empty tower is adopted for spraying, the spray layers are 3, the distance between every two layers is 1 meter, the circulating oil is cooled by circulating cooling water, the oil temperature after cooling is 130 ℃, a liquid separation tank is arranged behind the spray tower and integrated with the spray tower, and a silk screen demister is arranged at the outlet of the liquid separation tank. The circulating oil filter adopts a metal sintered filter, and the precision is 10 microns. The amount of recovered oil was measured to be 22% of the feed sludge.
d. The pyrolysis tail gas after oil removal and dust removal is pressurized by a fan and is sent into an incinerator, the pyrolysis tail gas and combustion-supporting air are mixed and combusted in the incinerator, the temperature of the incinerator is 950 ℃, the incinerator is connected with a waste boiler, the temperature of the tail gas of the incinerator is reduced to 380 ℃, and meanwhile low-pressure steam is a byproduct.
e. 380 ℃ of incinerator tail gas enters an SCR denitration reactor, 2 layers of high-temperature denitration catalysts are filled in the denitration reactor, and ammonia is sprayed in front of the denitration reactor to serve as a denitration reducing agent.
f. And (3) the denitrated waste gas enters a waste heat boiler to produce low-pressure steam as a byproduct, the temperature of the waste gas is reduced to 170 ℃, and then the waste gas enters a desulfurization tower.
g. The desulfurizing tower adopts a packed tower, a packing layer is arranged in the packed tower, a centrifugal pump is used as a conveying pump of the desulfurizing circulating liquid, NaOH is used as a desulfurizing agent, the PH value of the desulfurizing circulating liquid is kept to be about 8, and SO in the exhaust gas discharged by the desulfurizing tower2The concentration is less than 40mg/m3，NOxThe concentration is less than 50mg/m3。
h. And cooling the residue discharged from the pyrolysis furnace to 150 ℃ by a slag cooler, then feeding the residue into an ash hopper under the action of gravity, and discharging the residue according to the material level, wherein the cooling medium of the slag cooler is circulating cooling water. The amount of sludge accounted for 40% of the sludge feed, and the analyzed sludge had the following composition: 0.29 percent of sulfur, 81.39 percent of carbon, 11.84 percent of ash, 0.95 percent of water, 6.67 percent of dry ash-free base volatile matter and 29.20Mj/kg of heat value of a bullet.
i. Flue gas generated by heating and burning outside the pyrolysis furnace enters a waste boiler for energy recovery, low-pressure steam is generated as a byproduct, the temperature of the flue gas at the outlet of the waste boiler is 145 ℃, and the flue gas is pumped and sent to a chimney by a fan to be discharged.
According to the embodiment, through the treatment of units such as pyrolysis, oil recovery, pyrolysis tail gas incineration, waste heat recovery, denitration and desulfurization, products such as oil and coke and heat energy are effectively recovered, water in sludge and gas generated in the treatment process are discharged up to the standard, and the resource utilization of oily sludge is realized. The method and the device have the advantages of low operation cost, high emission standard, long-period safe and stable operation, and obvious economic benefit and environmental benefit.
While the present invention has been described with reference to exemplary embodiments, it is understood that the terminology used is intended to be in the nature of words of description and illustration, rather than of limitation. As the present invention may be embodied in several forms without departing from the spirit or essential characteristics thereof, it should also be understood that the above-described embodiments are not limited by any of the details of the foregoing description, but rather should be construed broadly within its spirit and scope as defined in the appended claims, and therefore all changes and modifications that fall within the meets and bounds of the claims, or equivalences of such meets and bounds are therefore intended to be embraced by the appended claims.
Claims (14)
1. An oily sludge treatment apparatus for treating the oily sludge, characterized by comprising:
the conveying unit is used for storing and conveying the oily sludge;
the pyrolysis unit is connected with the conveying unit and is used for carrying out pyrolysis treatment on the conveyed oily sludge;
the oil recovery unit is connected with the pyrolysis unit and used for dedusting pyrolysis process gas generated by the pyrolysis unit and cooling and recovering oil in the pyrolysis process gas;
the incineration unit is connected with the oil recovery unit and is used for carrying out incineration treatment on the waste gas subjected to dust removal and oil removal by the oil recovery unit; and
and the residue recovery unit is connected with the pyrolysis unit and used for cooling and recovering the solid residue generated by the pyrolysis unit.
2. The oily sludge treatment apparatus as claimed in claim 1, wherein the pyrolysis unit comprises an external heating type rotary furnace; preferably, the pyrolysis unit is connected with the waste heat recovery unit.
3. The oily sludge treatment apparatus according to claim 1 wherein the oil recovery unit comprises a spray tower, an oil circulation spray system, a circulating oil filtration system and a circulating oil cooling system.
4. The oily sludge treatment device according to claim 3, wherein the oil recovery unit further comprises a liquid separation system for separating liquid droplets entrained in the waste gas after the spraying oil removal.
5. The processing apparatus according to claim 1, wherein the residue recovery unit comprises a slag cooler, an ash hopper and an ash hopper discharge valve, and the ash hopper is provided with a level meter for opening and closing the discharge valve according to the level of the residue in the ash hopper.
6. The treatment device according to claim 1, wherein the oily sludge treatment device further comprises a waste heat recovery unit, and the waste heat recovery unit is connected with the incineration unit and used for cooling the incineration tail gas of the incineration unit and recovering heat energy thereof.
7. The treatment device according to claim 6, wherein the oily sludge treatment device further comprises an incineration exhaust gas denitration unit and/or desulfurization unit, and the incineration exhaust gas denitration and/or desulfurization unit is connected with the waste heat recovery unit and is used for carrying out denitration and/or desulfurization treatment on the exhaust gas of the waste heat recovery unit.
8. A method for treating oily sludge, which is used for treating the oily sludge, and is characterized by comprising the following steps:
a conveying step of storing and conveying the oily sludge;
a pyrolysis step of subjecting the oily sludge conveyed in the conveying step to pyrolysis treatment;
an oil recovery step, wherein the pyrolysis process gas generated in the pyrolysis step is subjected to dust removal and is cooled to recover oil in the pyrolysis process gas;
an incineration step, wherein the waste gas after dust and oil removal in the oil recovery step is incinerated; and
and a residue recovery step of cooling and recovering the solid residue generated in the pyrolysis step.
9. The method for treating oily sludge according to claim 8, wherein the pyrolysis step is performed in an oxygen-free atmosphere, and the pyrolysis temperature is 200-800 ℃, preferably 300-750 ℃, and more preferably 400-700 ℃.
10. The oil-containing sludge treatment method according to claim 8, wherein the oil recovery step uses the recovered oil as a circulating spray medium for recycling, and filters and cools the circulating oil; preferably, the filtration precision is 5-100 microns.
11. The oil-containing sludge treatment method according to claim 10, wherein the temperature of both the gas and the circulating oil in the oil recovery step is higher than the boiling point of water; preferably 100 to 130 ℃.
12. The method according to claim 8, wherein the exhaust gas from the oil recovery step to the incineration step is accompanied by heat.
13. The oily sludge treatment method according to claim 8, wherein the oily sludge treatment method further comprises a waste heat recovery step of subjecting the incineration exhaust gas generated in the incineration step to a temperature reduction treatment; the temperature of the gas after waste heat recovery is 100-400 ℃, and more preferably 220-380 ℃.
14. The method for treating oily sludge according to claim 8, wherein the method for treating oily sludge further comprises a step of denitration and/or desulfurization of incineration exhaust gas, and the denitration and/or desulfurization treatment is performed on the exhaust gas generated in the step of recovering waste heat of the incineration exhaust gas.
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| CN113308266A (en) * | 2021-06-10 | 2021-08-27 | 镇江新区固废处置股份有限公司 | Oil-containing solid waste disposal system based on pyrolysis technology |
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