CN211060139U - Pressurized fluidized bed oily sludge incineration system - Google Patents
Pressurized fluidized bed oily sludge incineration system Download PDFInfo
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Abstract
A pressurized fluidized bed oily sludge incineration system comprises an incinerator, an oil sludge receiving system, an oil sludge storage system, an odor collecting/pressurizing system, a pressurized combustion air supply system, a pressurized combustion air preheating system, a fuel supply system, a first combustor, a second combustor, a medium-temperature wet flue gas denitration and dust removal integrated system, a waste heat recovery system, a flue gas pressure reduction system, a flue gas dehumidification system, a flue gas discharge system, a fly ash discharge storage system and a fly ash resource utilization system, pressurized air is introduced into the fluidized bed incinerator, pressurized combustion is added into the incinerator, and high-temperature pressurized wet flue gas generated in the incinerator is cooled into medium-temperature pressurized wet flue gas; the process is characterized in that the process is carried out continuously to remove dust and denitrate to form medium-temperature pressurized clean wet flue gas, sensible heat of the flue gas is recycled through a waste heat recovery system, the oily sludge realizes reduction, harmlessness and resource utilization, energy conservation and emission reduction, combustion efficiency is improved, unit area treatment capacity of equipment is improved, and emission of harmful substances in the flue gas is reduced.
Description
Technical Field
The utility model belongs to the technical field of the oily sludge treatment, concretely relates to pressurized fluidized bed oily sludge system of burning.
Background
The oily sludge is mainly oil sludge and oil sand produced in the petroleum exploration and development industry and the petrochemical industry, has very complex components, contains a large amount of aged crude oil, salts, solid suspended matters, corrosion products, bacteria and the like, and also contains a large amount of water treatment agents added in the production process. The oily sludge has the characteristics of large production amount, large volume, high oil content, large treatment difficulty, few comprehensive utilization modes and the like, and if the oily sludge is not treated, the oily sludge pollutes the environment. Therefore, reduction, detoxification and recycling of the oily sludge are required.
At present, the treatment methods of the oily sludge mainly comprise the following steps: landfill, conditioning-mechanical separation, biological, thermal desorption, extraction, incineration, and the like.
The landfill method is to landfill the oily sludge in a suitable place selected on land, the method is the simplest, oldest and most primitive treatment method, the process is simple, the cost is low, but a large amount of land resources are occupied, if the protection measures are not perfect enough, the pollution to the environment is great, the sludge is buried underground, the total amount is not reduced, useful resources are not utilized, and the method cannot realize reduction, harmlessness and reduction treatment; the thermal refining-mechanical separation method is to select proper medicament to carry out optimized thermal refining treatment to improve the dehydration effect, and then to dehydrate in a mechanical mode, the method can improve the dehydration effect and carry out reduction treatment, but can not effectively carry out further treatment and can not realize harmless treatment and recycling treatment; the thermal pyrolysis separation method is to heat the oily sludge in an anaerobic environment to pyrolyze hydrocarbons and organic matters so as to realize oil-sludge separation, hydrocarbon, micromolecular combustible gas and liquid can be recycled, and the high potential heat value of the hydrocarbon, micromolecular combustible gas and liquid is effectively utilized, the method cannot realize reduction, harmlessness and reduction treatment, but the reaction of the process is generally carried out at high temperature, the reaction condition requirement is higher, the operation is more complex, and the method is not widely used at present in China; the biological method is characterized in that oily substances in sludge are used as a carbon source of microorganisms, and are subjected to biochemical degradation in certain environment and condition to be completely converted into harmless inorganic substances. The solvent extraction method is a method for extracting and recovering oil substances in the oily sludge by using a solvent extraction agent, can recover and utilize effective components in the oily sludge, has good treatment effect, consumes a large amount of solvent, has high cost, and easily causes secondary pollution by treated waste liquid. The incineration method is characterized in that firstly, the oily sludge is dried to remove most of moisture in the sludge, and then the dried sludge is incinerated, the method not only can reduce and harmlessly treat the sludge, but also can recover resources in the sludge in a heat mode to realize resource utilization, and the treatment process is simple, the equipment investment and the operation cost are low, so that the method is a main oily sludge treatment method at present.
At present, the incineration method mainly comprises a rotary kiln incineration method, a fluidized bed incineration method and the like, for example, patents CN208025528U, CN108298796A, CN203036646U and CN207407355U all adopt a rotary kiln method, the method has mature technology and strong sludge adaptability, sludge is treated more thoroughly, resources in the sludge can be recycled in a hot form, but the method has the defects of low thermal efficiency, large floor area, small single-equipment treatment capacity, high equipment investment and operation cost and the like; the CN207674458U patent adopts a normal-pressure fluidized bed burning method, the method has the advantages of simple equipment, high reaction mass and heat transfer efficiency, high combustion efficiency and larger treatment capacity of unit area of the equipment, is particularly suitable for oily sludge with higher water content, but needs to supplement more energy, has higher ash content, higher content of nitrogen sulfide in flue gas and smaller treatment capacity although the treatment capacity of the unit area of the equipment is improved.
Therefore, the research on how to effectively burn the oily sludge so as to better realize reduction, harmless treatment and resource treatment has very important practical significance.
Disclosure of Invention
In order to overcome the defects of the prior art, the utility model aims to provide a pressurized fluidized bed oily sludge incineration system, through the system, oily sludge is changed into smoke and fly ash after incineration, so that the amount of solid waste is reduced by more than 5 percent, and the reduction treatment is realized; meanwhile, the flue gas is purified and discharged up to the standard, and basically has no pollution to the environment, and the fly ash is made into industrial bricks, so that the environment is not polluted, and the harmless treatment of the oily sludge is realized; the waste heat generated after the oily sludge is burnt is converted into saturated steam to be used as a steam source, the fly ash is also made into industrial bricks, and the oily sludge is recycled; the carbon content of the fly ash produced by the technologies such as a normal-pressure fluidized bed and the like is reduced by about 1 percent, the combustion efficiency is high, the carbon conversion rate is higher than 99 percent and is about 5 percent higher than that of other technologies, the energy recovery rate can reach 88 percent, the discharge amount of nitrogen oxides in the produced flue gas is reduced by about 18 percent compared with that of the traditional technology, and the oily sludge is effectively treated so as to realize reduction, harmless and resource treatment.
In order to realize the purpose, the utility model discloses a technical scheme is:
the utility model provides a pressurized fluidized bed oily sludge incineration system, includes incinerator 1, fatlute receiving system 2, fatlute jar stores up system 3, foul smell collection/pressurization system 4, pressurized combustion air supply system 5, pressurized combustion air preheats system 6, supplies fuel system 7, first combustor 8, second combustor 9, medium temperature wet flue gas denitration dust removal integrated system 10, waste heat recovery system 11, flue gas decompression system 12, flue gas system 13 that falls wet, flue gas discharge system 14, fly ash discharge jar stores up system 15 and fly ash resource utilization system 16:
the incinerator 1 is provided with a main combustion air inlet 1-1, an oily sludge inlet 1-2 of the incinerator, a first flue gas inlet 1-3, a second flue gas inlet 1-4, an odor inlet 1-5 and a high-temperature pressurized wet flue gas outlet 1-6, wherein the main combustion air inlet 1-1 is communicated with a high-temperature pressurized air outlet 6-3 of a pressurized combustion air preheating system 6, a fuel outlet 7-1 of a fuel supply system 7, a mixed combustion matter inlet 8-1 of a first combustor 8 and a mixed combustion matter inlet 9-1 of a second combustor 9; an oily sludge inlet 1-2 of the incinerator is communicated with a second oily sludge outlet 2-4 of the oil sludge receiving system 2 and an oily sludge outlet 3-3 of the oil sludge storage system 3; the first flue gas inlet 1-3 is communicated with a flue gas outlet 8-2 of the first combustor 8; the second flue gas inlet 1-4 is communicated with a flue gas outlet 9-2 of a second combustor 9; the odor inlet 1-5 is communicated with the odor outlet 4-3 of the odor collecting/pressurizing system 4; the high-temperature pressurized wet flue gas outlet 1-6 is communicated with a high-temperature pressurized wet flue gas inlet 6-2 of the pressurized combustion air preheating system 6;
the oil sludge receiving system 2 is provided with an oily sludge inlet 2-1, a first oily sludge outlet 2-2, an odor outlet 2-3 and a second oily sludge outlet 2-4 of the oil sludge receiving system, wherein the oily sludge inlet 2-1 of the oil sludge receiving system is communicated with an oily sludge source, the first oily sludge outlet 2-2 is communicated with an oily sludge inlet 3-1 of an oil sludge storage system of the oil sludge storage system 3, the odor outlet 2-3 of the oil sludge receiving system is communicated with a first odor inlet 4-1 of an odor collecting/pressurizing system 4, and the second oily sludge outlet 2-4 is communicated with an oily sludge outlet 3-3 of the oil sludge storage system 3;
the oil sludge storage system 3 is provided with an oily sludge inlet 3-1 of the oil sludge storage system, an odor outlet 3-2 of the oil sludge storage system and an oily sludge outlet 3-3, and the odor outlet 3-2 of the oil sludge storage system is communicated with a second odor inlet 4-2 of the odor collecting/pressurizing system 4;
the pressurized combustion air preheating system 6 is provided with a low-temperature pressurized air inlet 6-1, a high-temperature pressurized wet flue gas inlet 6-2, a high-temperature pressurized air outlet 6-3 and a warm pressurized wet flue gas outlet 6-4, wherein the low-temperature pressurized air inlet 6-1 is communicated with a low-temperature pressurized air outlet 5-1 of the pressurized combustion air supply system 5, and the warm pressurized wet flue gas outlet 6-4 is communicated with a medium-temperature pressurized clean wet flue gas inlet 10-1 of the medium-temperature wet flue gas denitration and dust removal integrated system 10;
the fuel outlet 7-1 of the fuel supply system 7 is communicated with the mixed combustion material inlet 8-1 of the first combustor 8 and the mixed combustion material inlet 9-1 of the second combustor 9;
the medium-temperature wet flue gas denitration and dust removal integrated system 10 is provided with a medium-temperature pressurized clean wet flue gas inlet 10-1, a medium-temperature pressurized clean flue gas outlet 10-2 and a fly ash outlet 10-3, wherein the medium-temperature pressurized clean flue gas outlet 10-2 is communicated with a medium-temperature pressurized clean flue gas inlet 11-1 of a waste heat recovery system 11; the fly ash outlet 10-3 is communicated with a fly ash inlet 15-1 of a fly ash discharge tank storage system 15;
a fly ash outlet 15-2 of the fly ash discharge tank storage system 15 is communicated with a fly ash inlet 16-1 of a fly ash resource utilization system 16;
the low-temperature pressurized clean wet flue gas outlet 11-2 of the waste heat recovery system 11 is communicated with the low-temperature pressurized clean wet flue gas inlet 12-1 of the flue gas pressure reduction system 12;
the low-temperature normal-pressure clean wet flue gas outlet 12-2 of the flue gas pressure reduction system 12 and the low-temperature normal-pressure clean wet flue gas inlet 13-1 of the flue gas dehumidification system 13 are connected in series;
the low-temperature normal-pressure clean dry flue gas outlet 13-2 of the flue gas dehumidification system 13 is communicated with the low-temperature normal-pressure clean dry flue gas inlet 14-1 of the flue gas discharge system 14.
The incinerator 1 is a pressurized fluidized bed incinerator, and a pressurized bubbling fluidized bed reactor is adopted.
The fuel of the fuel supply system 7 can adopt oil or gas.
The charging opening of the incinerator 1 can be located in the dilute phase zone at the upper part of the hearth, and can also be located in the dense phase zone at the lower part of the hearth.
The medium-temperature wet flue gas denitration and dust removal integrated system 10 is a high-temperature integrated system.
The system comprises an incinerator 1, an oil sludge receiving system 2, an oil sludge storage system 3, an odor collecting/pressurizing system 4, a pressurized combustion air supply system 5, a pressurized combustion air preheating system 6, a fuel supply system 7, a first combustor 8, a second combustor 9, a medium-temperature and wet flue gas denitration and dust removal integrated system 10, a waste heat recovery system 11, a flue gas pressure reduction system 12, a flue gas dehumidification system 13, a flue gas discharge system 14, a fly ash discharge storage system 15 and a resource fly ash utilization system 16.
A method for incinerating oily sludge by pressurized fluidized bed comprises the following steps:
1) an oily sludge raw material A from an oily sludge source enters a sludge receiving system 2 and then is transported to a sludge storage system 3 to be stored for later use, wherein in the receiving and storing process, odor B volatilized from the sludge receiving system 2 and the sludge storage system 3 is collected by an odor collecting/pressurizing system 4 and is discharged from the odor collecting/pressurizing system 4, and the discharged odor B enters an incinerator 1 to be incinerated;
2) the low-temperature pressurized air C generated by the pressurized combustion air supply system 5 enters the pressurized combustion air preheating system 6 and exchanges heat with the high-temperature pressurized wet flue gas G from the incinerator 1, and the low-temperature pressurized air C is heated into high-temperature pressurized air D and is discharged from the pressurized combustion air preheating system 6; meanwhile, the high-temperature pressurized wet flue gas G is cooled into medium-temperature pressurized wet flue gas P with lower temperature and is discharged from the pressurized combustion air preheating system 6;
3) a part of gas in high-temperature pressurized air D discharged from the pressurized combustion air preheating system 6 is introduced into the incinerator 1 as main combustion air F, and under the pneumatic action of the main combustion air F, a fluidizing medium in the incinerator 1 is in a high-temperature bubbling fluidizing state; the high-temperature bubbling fluidization state is that the gas velocity of the fluidized bed is 0.1-2 m/s, the pressure in the pressurized fluidized bed is 0.1-0.5 MPa, and the incineration temperature is 750-;
4) supplying the volatilized odor F into the incinerator 1 from the oil sludge storage system 3 or directly from the oil sludge receiving system 2 at a certain speed through a mechanical pump while introducing the main combustion air F into the incinerator 1, wherein the volatilized odor oily sludge F enters the incinerator 1 to be mixed with the gas E and then undergoes a combustion reaction at a high temperature to generate high-temperature pressurized wet flue gas G, and the high-temperature pressurized wet flue gas G is discharged from the incinerator 1;
5) when the oily sludge has a low heat value and can not realize self-heating and the incinerator is started, fuel H can be introduced into the first combustor 8 and the second combustor 9 from the fuel supply system 7, the fuel H and part of high-temperature pressurized air E from the pressurized combustion air preheating system 6 are mixed into mixed combustion products K and L as combustor combustion air J and are combusted in the first combustor 8 and the second combustor 9 respectively, and flue gas M and flue gas N generated by combustion are directly sprayed into the incinerator 1 to supplement the required heat for combustion;
6) the high-temperature pressurized wet flue gas G discharged from the incinerator 1 enters a pressurized combustion air preheating system 6, exchanges heat with high-temperature pressurized air D, is cooled into medium-temperature pressurized wet flue gas P and is discharged from the pressurized combustion air preheating system 6;
7) the medium temperature pressurized wet flue gas P discharged from the pressurized combustion air preheating system 6 enters the medium temperature wet flue gas denitration and dust removal integrated system 10, is subjected to purification treatment such as denitration/dust removal to become medium temperature pressurized clean wet flue gas Q and is discharged from the medium temperature wet flue gas denitration and dust removal integrated system 10, and simultaneously, fly ash R removed from the flue gas is also discharged from the medium temperature wet flue gas denitration and dust removal integrated system 10; the temperature during denitration and dust removal is 400-700 ℃;
8) the medium-temperature pressurized clean wet flue gas Q discharged from the medium-temperature wet flue gas denitration and dust removal integrated system 10 enters a waste heat recovery system 11, heat exchange is carried out between the medium-temperature pressurized clean wet flue gas Q and a cooling medium, the medium-temperature pressurized clean wet flue gas Q is cooled to be low-temperature pressurized clean wet flue gas T so as to recover waste heat, and the low-temperature pressurized clean wet flue gas S is discharged from the waste heat recovery system 11 after heat exchange;
9) the low-temperature pressurized clean wet flue gas S discharged from the waste heat recovery system 11 enters the flue gas pressure reduction system 12 to be reduced into low-temperature normal-pressure clean wet flue gas T and is discharged from the flue gas pressure reduction system 12;
10) the pressure reduced clean wet flue gas T discharged from the flue gas pressure reduction system 12 enters the flue gas humidity reduction system 13, is subjected to humidity reduction treatment to form clean dry flue gas U at low temperature and normal pressure, and is discharged from the flue gas humidity reduction system 13.
11) The low-temperature normal-pressure clean dry flue gas U discharged from the flue gas dehumidification system 13 enters the flue gas discharge system 14 after reaching the standard and is discharged;
12) the fly ash S discharged from the medium-temperature and wet flue gas denitration and dust removal integrated system 10 enters a fly ash discharge tank storage system 15 for storage, and is discharged after being accumulated in a sufficient amount and enters a fly ash resource utilization system 16 for resource utilization;
the medium-temperature and wet flue gas denitration and dust removal integrated system 10 adopts a high-temperature-resistant ceramic fiber pipe with a denitration catalyst as a filter material.
When the calorific value of the oily sludge in the oil field is higher, the system does not adopt the fuel supply system 7, the first combustor 8 and the second combustor 9.
The utility model has the advantages that:
1. by adopting the patent of the utility model, the oil-containing sludge realizes the harmlessness, the reduction and the resource utilization;
2. because of adopting the pressurized combustion mode, the air quantity in the unit volume in the incinerator is multiplied, the air quantity is sufficient, the treatment capacity of the equipment in unit area can be greatly improved, and the treatment capacity can be improved by more than 8 times at most;
3. the pressure is higher, the oxygen content in unit volume of the equipment is higher, so that the oil-containing sludge is fully contacted with air, the combustion is more sufficient, and the efficiency is higher;
4. the discharge amount of nitrogen oxides in the flue gas of the incineration technology of the utility model is greatly reduced by 20 percent at most;
5. the residue after the oily sludge is combusted is discharged in the form of fly ash and is intensively treated and utilized, so that the discharge amount of the fly ash is reduced, and the fly ash is recycled;
6. the flue gas after oily sludge incineration adopts a mode of integrating dust removal and denitration at high temperature, so that two processes are integrated in one unit, the treatment efficiency is higher, and the equipment investment and the operation investment are reduced.
For review, through the system incineration treatment of the method, the oily sludge is changed into smoke and fly ash after incineration, so that the amount of solid waste is reduced by more than 5 percent of the original amount, and the reduction treatment is realized; meanwhile, the flue gas is purified and discharged up to the standard, and basically has no pollution to the environment, and the fly ash is made into industrial bricks, so that the environment is not polluted, and the harmless treatment of the oily sludge is realized; the waste heat generated after the oily sludge is burnt is converted into saturated steam to be used as a steam source, the fly ash is also made into industrial bricks, and the oily sludge is recycled; the carbon content of the fly ash produced by the technologies such as a normal-pressure fluidized bed and the like is reduced by about 1 percent, the combustion efficiency is high, the carbon conversion rate is higher than 99 percent and is about 5 percent higher than that of other technologies, the energy recovery rate can reach 88 percent, the discharge amount of nitrogen oxides in the produced flue gas is reduced by about 18 percent compared with that of the traditional technology, and the oily sludge is effectively treated so as to realize reduction, harmless and resource treatment.
Drawings
Fig. 1 is a schematic diagram of the system structure principle of the present invention.
Fig. 2 is a working principle diagram of the present invention.
Fig. 3 is a schematic diagram of a system structure principle of embodiment 2 of the present invention.
Fig. 4 is a working principle diagram of embodiment 2 of the present invention.
The fly ash recycling system comprises an incinerator 1, a main combustion air inlet 1-1, an oil-containing sludge inlet 1-2, a first flue gas inlet 1-3, a second flue gas inlet 1-4, an odor inlet 1-5, a high-temperature pressurized flue gas outlet 1-6, an oil sludge receiving system 2-1, an oil sludge inlet 2-2, a first oil-containing sludge outlet 2-3, an odor outlet 2-4, an oil sludge storage system 3-1, an oil sludge inlet 3-2, an odor outlet 3-3, an oil sludge outlet 4, an odor collecting/pressurizing system 4-1, a first odor inlet 4-2, a second odor inlet 4-3, an odor outlet 5, a pressurized combustion air supply system 5-1, a low-temperature pressurized air outlet 6, a pressurized combustion air preheating system 6-1, a low-temperature pressurized air inlet 6-2, a high-temperature pressurized combustion air inlet 6-2, a high-temperature pressurized flue gas inlet 6-10, a high-temperature pressurized flue gas inlet 6, a normal-pressurized flue gas pressurized combustion air inlet 6-10, a high-temperature pressurized flue gas inlet 6-pressurized flue gas inlet, a high-pressurized flue gas inlet 10, a clean flue gas inlet 10, a high-pressurized flue gas inlet 3-pressurized flue gas inlet 10, a high-pressurized flue gas inlet 10, a clean wet flue gas inlet 3-pressurized flue gas inlet 3, a high-pressurized flue gas inlet, a high-pressurized flue gas inlet 3, a high-pressurized flue gas inlet 10, a fly ash pressurized flue gas inlet, a high-pressurized flue gas inlet, a clean wet flue gas inlet, a high-pressurized flue gas inlet 2, a high-pressurized flue gas inlet, a clean wet flue gas inlet, a clean air supply system, a clean wet flue gas inlet, a high-pressurized flue gas inlet, a clean air supply system, a high-pressurized flue gas inlet, a high-pressurized flue gas inlet, a high-pressurized flue gas inlet, a high-pressurized flue gas pressurized.
Detailed Description
The present invention will be further described with reference to the accompanying drawings and examples.
As shown in fig. 1, a pressurized fluidized bed oily sludge incineration system includes an incinerator 1 (for mixing and burning oil sludge and main fuel air to generate heat), an oil sludge receiving system 2 (for temporary storage and conditioning of oil sludge), an oil sludge storage system 3 (for storing and maintaining stable feeding of oil sludge), an odor collecting/pressurizing system 4 (for collecting and pressurizing harmful gas overflowed from production sites and devices), a pressurized combustion air supply system 5 (for supplying pressurized air during start-up of a vehicle), a pressurized combustion air preheating system 6 (for preheating air for combustion and cooling high-temperature flue gas), a fuel supply system 7 (for supplying insufficient fuel during start-up and operation of the incinerator), a first burner 8 (for supplying heat to the incinerator for temperature rise and stable operation), a second burner 9 (for supplying heat to the incinerator for temperature rise and stable operation) and a second burner 9 (for supplying heat to the incinerator for heat rise and stable operation) are provided, The integrated system 10 for medium temperature and humidity flue gas denitration and dust removal (for removing harmful substances such as smoke dust and NOx in flue gas), the waste heat recovery system 11 (for recovering heat in flue gas), the flue gas pressure reduction system 12 (for reducing the pressure of pressurized flue gas to normal pressure), the flue gas humidity reduction system 13 (for reducing the humidity of flue gas to meet the requirement of flue gas emission), the flue gas emission system 14 (for flue gas standard emission and monitoring devices), the fly ash discharge tank storage system 15 (for collecting fly ash generated by flue gas dust removal) and the fly ash recycling system 16 (for fly ash recycling treatment device):
the incinerator 1 is provided with a main combustion air inlet 1-1, an oily sludge inlet 1-2 of the incinerator, a first flue gas inlet 1-3, a second flue gas inlet 1-4, an odor inlet 1-5 and a high-temperature pressurized wet flue gas outlet 1-6, wherein the main combustion air inlet 1-1 is communicated with a high-temperature pressurized air outlet 6-3 of a pressurized combustion air preheating system 6, a fuel outlet 7-1 of a fuel supply system 7, a mixed combustion matter inlet 8-1 of a first combustor 8 and a mixed combustion matter inlet 9-1 of a second combustor 9; an oily sludge inlet 1-2 of the incinerator is communicated with a second oily sludge outlet 2-4 of the oil sludge receiving system 2 and an oily sludge outlet 3-3 of the oil sludge storage system 3; the first flue gas inlet 1-3 is communicated with a flue gas outlet 8-2 of the first combustor 8; the second flue gas inlet 1-4 is communicated with a flue gas outlet 9-2 of a second combustor 9; the odor inlet 1-5 is communicated with the odor outlet 4-3 of the odor collecting/pressurizing system 4; the high-temperature pressurized wet flue gas outlet 1-6 is communicated with a high-temperature pressurized wet flue gas inlet 6-2 of the pressurized combustion air preheating system 6;
the oil sludge receiving system 2 is provided with an oily sludge inlet 2-1, a first oily sludge outlet 2-2, an odor outlet 2-3 and a second oily sludge outlet 2-4 of the oil sludge receiving system, wherein the oily sludge inlet 2-1 of the oil sludge receiving system is communicated with an oily sludge source, the first oily sludge outlet 2-2 is communicated with an oily sludge inlet 3-1 of an oil sludge storage system of the oil sludge storage system 3, the odor outlet 2-3 of the oil sludge receiving system is communicated with a first odor inlet 4-1 of an odor collecting/pressurizing system 4, and the second oily sludge outlet 2-4 is communicated with an oily sludge outlet 3-3 of the oil sludge storage system 3;
the oil sludge storage system 3 is provided with an oily sludge inlet 3-1 of the oil sludge storage system, an odor outlet 3-2 of the oil sludge storage system and an oily sludge outlet 3-3, and the odor outlet 3-2 of the oil sludge storage system is communicated with a second odor inlet 4-2 of the odor collecting/pressurizing system 4;
the pressurized combustion air preheating system 6 is provided with a low-temperature pressurized air inlet 6-1, a high-temperature pressurized wet flue gas inlet 6-2, a high-temperature pressurized air outlet 6-3 and a warm pressurized wet flue gas outlet 6-4, wherein the low-temperature pressurized air inlet 6-1 is communicated with a low-temperature pressurized air outlet 5-1 of the pressurized combustion air supply system 5, and the warm pressurized wet flue gas outlet 6-4 is communicated with a medium-temperature pressurized clean wet flue gas inlet 10-1 of the medium-temperature wet flue gas denitration and dust removal integrated system 10;
the fuel outlet 7-1 of the fuel supply system 7 is communicated with the mixed combustion material inlet 8-1 of the first combustor 8 and the mixed combustion material inlet 9-1 of the second combustor 9;
the medium-temperature wet flue gas denitration and dust removal integrated system 10 is provided with a medium-temperature pressurized clean wet flue gas inlet 10-1, a medium-temperature pressurized clean flue gas outlet 10-2 and a fly ash outlet 10-3, wherein the medium-temperature pressurized clean flue gas outlet 10-2 is communicated with a medium-temperature pressurized clean flue gas inlet 11-1 of a waste heat recovery system 11; the fly ash outlet 10-3 is communicated with a fly ash inlet 15-1 of a fly ash discharge tank storage system 15;
a fly ash outlet 15-2 of the fly ash discharge tank storage system 15 is communicated with a fly ash inlet 16-1 of a fly ash resource utilization system 16;
the low-temperature pressurized clean wet flue gas outlet 11-2 of the waste heat recovery system 11 is communicated with the low-temperature pressurized clean wet flue gas inlet 12-1 of the flue gas pressure reduction system 12;
the low-temperature normal-pressure clean wet flue gas outlet 12-2 of the flue gas pressure reduction system 12 and the low-temperature normal-pressure clean wet flue gas inlet 13-1 of the flue gas dehumidification system 13 are connected in series;
the low-temperature normal-pressure clean dry flue gas outlet 13-2 of the flue gas dehumidification system 13 is communicated with the low-temperature normal-pressure clean dry flue gas inlet 14-1 of the flue gas discharge system 14.
The incinerator 1 is a pressurized fluidized bed incinerator, and a pressurized bubbling fluidized bed reactor is adopted.
The fuel of the fuel supply system 7 can adopt oil or gas.
The charging opening of the incinerator 1 can be located in the dilute phase zone at the upper part of the hearth, and can also be located in the dense phase zone at the lower part of the hearth.
The medium-temperature wet flue gas denitration and dust removal integrated system 10 is a high-temperature integrated system.
The system comprises an incinerator 1, an oil sludge receiving system 2, an oil sludge storage system 3, an odor collecting/pressurizing system 4, a pressurized combustion air supply system 5, a pressurized combustion air preheating system 6, a fuel supply system 7, a first combustor 8, a second combustor 9, a medium-temperature and wet flue gas denitration and dust removal integrated system 10, a waste heat recovery system 11, a flue gas pressure reduction system 12, a flue gas dehumidification system 13, a flue gas discharge system 14, a fly ash discharge storage system 15 and a resource fly ash utilization system 16
As shown in fig. 2, a method for incinerating oily sludge in a pressurized fluidized bed comprises the following steps:
1) an oily sludge raw material A from an oily sludge source enters a sludge receiving system 2 and then is transported to a sludge storage system 3 to be stored for later use, wherein in the receiving and storing process, odor B volatilized from the sludge receiving system 2 and the sludge storage system 3 is collected by an odor collecting/pressurizing system 4 and is discharged from the odor collecting/pressurizing system 4, and the discharged odor B enters an incinerator 1 to be incinerated;
2) the low-temperature pressurized air C generated by the pressurized combustion air supply system 5 enters the pressurized combustion air preheating system 6 and exchanges heat with the high-temperature pressurized wet flue gas G from the incinerator 1, and the low-temperature pressurized air C is heated into high-temperature pressurized air D and is discharged from the pressurized combustion air preheating system 6; meanwhile, the high-temperature pressurized wet flue gas G is cooled into medium-temperature pressurized wet flue gas P with lower temperature and is discharged from the pressurized combustion air preheating system 6;
3) a part of gas in high-temperature pressurized air D discharged from the pressurized combustion air preheating system 6 is introduced into the incinerator 1 as main combustion air F, and under the pneumatic action of the main combustion air F, a fluidizing medium in the incinerator 1 is in a high-temperature bubbling fluidizing state; the high-temperature bubbling fluidization state is that the gas velocity of the fluidized bed is 0.1-2 m/s, the pressure in the pressurized fluidized bed is 0.1-0.5 MPa, and the incineration temperature is 750-;
4) supplying the volatilized odor F into the incinerator 1 from the oil sludge storage system 3 or directly from the oil sludge receiving system 2 at a certain speed through a mechanical pump while introducing the main combustion air F into the incinerator 1, wherein the volatilized odor oily sludge F enters the incinerator 1 to be mixed with the gas E and then undergoes a combustion reaction at a high temperature to generate high-temperature pressurized wet flue gas G, and the high-temperature pressurized wet flue gas G is discharged from the incinerator 1;
5) when the oily sludge has a low heat value and can not realize self-heating and the incinerator is started, fuel H can be introduced into the first combustor 8 and the second combustor 9 from the fuel supply system 7, the fuel H and part of high-temperature pressurized air E from the pressurized combustion air preheating system 6 are mixed into mixed combustion products K and L as combustor combustion air J and are combusted in the first combustor 8 and the second combustor 9 respectively, and flue gas M and flue gas N generated by combustion are directly sprayed into the incinerator 1 to supplement the required heat for combustion;
6) the high-temperature pressurized wet flue gas G discharged from the incinerator 1 enters a pressurized combustion air preheating system 6, exchanges heat with high-temperature pressurized air D, is cooled into medium-temperature pressurized wet flue gas P and is discharged from the pressurized combustion air preheating system 6;
7) the medium temperature pressurized wet flue gas P discharged from the pressurized combustion air preheating system 6 enters the medium temperature wet flue gas denitration and dust removal integrated system 10, is subjected to purification treatment such as denitration/dust removal to become medium temperature pressurized clean wet flue gas Q and is discharged from the medium temperature wet flue gas denitration and dust removal integrated system 10, and simultaneously, fly ash R removed from the flue gas is also discharged from the medium temperature wet flue gas denitration and dust removal integrated system 10; the temperature during denitration and dust removal is 400-700 ℃;
8) the medium-temperature pressurized clean wet flue gas Q discharged from the medium-temperature wet flue gas denitration and dust removal integrated system 10 enters a waste heat recovery system 11, heat exchange is carried out between the medium-temperature pressurized clean wet flue gas Q and a cooling medium, the medium-temperature pressurized clean wet flue gas Q is cooled to be low-temperature pressurized clean wet flue gas T so as to recover waste heat, and the low-temperature pressurized clean wet flue gas S is discharged from the waste heat recovery system 11 after heat exchange;
9) the low-temperature pressurized clean wet flue gas S discharged from the waste heat recovery system 11 enters the flue gas pressure reduction system 12 to be reduced into low-temperature normal-pressure clean wet flue gas T and is discharged from the flue gas pressure reduction system 12;
10) the pressure reduced clean wet flue gas T discharged from the flue gas pressure reduction system 12 enters the flue gas humidity reduction system 13, is subjected to humidity reduction treatment to form clean dry flue gas U at low temperature and normal pressure, and is discharged from the flue gas humidity reduction system 13.
11) The low-temperature normal-pressure clean dry flue gas U discharged from the flue gas dehumidification system 13 enters the flue gas discharge system 14 after reaching the standard and is discharged;
12) the fly ash S discharged from the medium-temperature and wet flue gas denitration and dust removal integrated system 10 enters a fly ash discharge tank storage system 15 for storage, and is discharged after being accumulated in a sufficient amount and enters a fly ash resource utilization system 16 for resource utilization;
the medium-temperature and wet flue gas denitration and dust removal integrated system 10 adopts a high-temperature-resistant ceramic fiber pipe with a denitration catalyst as a filter material.
When the calorific value of the oily sludge in the oil field is higher, the system does not adopt the fuel supply system 7, the first combustor 8 and the second combustor 9.
Example 1
As shown in the combined drawings 1 and 2, oil field oil-containing sludge with lower heat value is adopted as a raw material, the water content is 85 percent, the heat value is 1500kcal/kg, and the sludge treatment capacity is 9 t/h.
The incineration process of the oily sludge is as follows:
1) an oily sludge raw material A from an oily sludge source is loaded into a sludge receiving system 2 and then transported to a sludge storage system 3 for storage and standby, wherein during the receiving and storing process, odor B volatilized from the sludge receiving system 2 and the sludge storage system 3 is collected by an odor collecting/pressurizing system 4 and discharged from the odor collecting/pressurizing system 4;
2) 20000 Nm generated by pressurized combustion air supply system 53The low-temperature pressurized air C with the temperature of 25 ℃ and the pressure of 0.3MPa enters the pressurized combustion air preheating system 6, exchanges heat with high-temperature pressurized wet flue gas G with the temperature of 850 ℃, the pressure of 0.3MPa and the nitrogen oxide content of 820 ppm from a fluidized bed incinerator (called incinerator for short) 1, is heated into high-temperature pressurized air D with the temperature of 170 ℃ and the pressure of 0.3MPa, and is discharged from the pressurized combustion air preheating system 6; meanwhile, the high-temperature pressurized wet flue gas G is cooled to the middle-temperature pressurized wet flue gas P with the temperature of 750 ℃, the pressure of 0.3MPa and the content of nitrogen oxides of 800 ppm and is discharged from the pressurized combustion air preheating system 6
3) 18000 Nm in high-temperature pressurized air D discharged from the pressurized combustion air preheating system 63And/h is used as main combustion air F and introduced into the incinerator 1, and the fluidizing medium in the incinerator 1 is in a fluidizing state at the temperature of 850 ℃ under the action of the air force of the main combustion air E.
4) Supplying oil-containing sludge F with volatilized odor from the oil sludge storage system 2 into the incinerator 1 at a feeding rate of 9 t/h while introducing main combustion air E into the incinerator 1, wherein the oil-containing sludge F with volatilized odor enters the incinerator 1 to be mixed with the main combustion air E and then undergoes a combustion reaction at a high temperature to generate high-temperature pressurized wet flue gas G with the temperature of 850 ℃, the pressure of 0.3MPa and the nitrogen oxide content of 820 ppm, and the high-temperature pressurized wet flue gas G is discharged from the incinerator 1;
5) when the calorific value of the oily sludge is lower and self-heating can not be realized,from the fuel supply system (oil/gas) 7 to the burners 8 and 9 at 190 Nm3H introduction of Fuel J, 2000 Nm of high-temperature gas mixture D from pressurized Combustion air preheating System 63The mixture of the air J serving as the burner is mixed into a mixed combustion object L and a mixed combustion object M which are respectively introduced into the burner 8 and the burner 9 for combustion, and the flue gas M and the flue gas N which are respectively generated after the combustion are introduced into the incinerator 1 for supplementing heat;
6) high-temperature pressurized wet flue gas H which is discharged from the incinerator 1 and has the temperature of 850 ℃, the pressure of 0.3MPa and the content of nitric oxide of 820 ppm enters a pressurized combustion air preheating system 6 to exchange heat with mixed gas C, is cooled to medium-temperature pressurized wet flue gas Q with the temperature of 750 ℃, the pressure of 0.3MPa and the content of nitric oxide of 800 ppm and is discharged from the pressurized combustion air preheating system 6;
7) the middle temperature pressurized wet flue gas P with the content of nitric oxide of 750 ℃, 0.3MPa and 800 ppm discharged from the pressurized combustion air preheating system 6 enters the middle temperature wet flue gas denitration and dust removal integrated system 10 to be purified into clean flue gas R with the content of nitric oxide of 750 ℃, 0.3MPa and 200 ppm by denitration and dust removal and the like, and is discharged from the middle temperature wet flue gas denitration and dust removal integrated system 10, and simultaneously, fly ash R with the content of 0.65% carbon at 0.20 t/h removed from the flue gas is also discharged from the middle temperature wet flue gas denitration and dust removal integrated system 10;
8) the medium-temperature pressurized clean wet flue gas Q discharged from the medium-temperature wet flue gas denitration and dust removal integrated system 10 enters a waste heat recovery system 11, heat exchange is carried out between a cooling medium and the medium-temperature pressurized clean wet flue gas Q, the medium-temperature pressurized clean wet flue gas Q is cooled to 250 ℃ and 0.3MPa, so as to recover the waste heat of the medium-temperature pressurized clean wet flue gas Q, 275 t/h of 60 ℃ hot water is generated, and the low-temperature pressurized clean wet flue gas S is discharged from the waste heat recovery system 11 after heat exchange;
9) the low-temperature pressurized clean wet flue gas S discharged from the waste heat recovery system 11 enters the flue gas pressure reduction system 12 to be reduced into low-temperature normal-pressure clean wet flue gas T and is discharged from the flue gas pressure reduction system 12;
10) the low-temperature normal-pressure clean wet flue gas T discharged from the flue gas pressure reduction system 12 enters the flue gas dehumidification system 13, is subjected to dehumidification and purification treatment to obtain low-temperature normal-pressure clean dry flue gas U with the temperature of 80 ℃ and the pressure of 0.3MPa, and is discharged from the flue gas dehumidification system 13;
11) the low-temperature normal-pressure clean dry flue gas U discharged from the flue gas dehumidification system 13 enters the flue gas discharge system 14 to be discharged after reaching the standard;
12) the fly ash R discharged from the medium-temperature and wet flue gas denitration and dust removal integrated system 10 enters the fly ash discharge tank storage system 15 for storage, and is discharged and added into the fly ash resource utilization system 16 for resource utilization after being accumulated in a sufficient amount.
By the embodiment, the oily sludge is incinerated, the oily sludge is changed into smoke and fly ash after incineration, and the residual residue after treatment is 0.20 t/h, so that the amount of solid waste is reduced to 6% of the original amount, and the reduction treatment is realized; meanwhile, the flue gas is purified and discharged up to the standard, and basically has no pollution to the environment, and the fly ash is made into industrial bricks, so that the environment is not polluted, and the harmless treatment of the oily sludge is realized; the waste heat generated after the oily sludge is burnt is converted into saturated steam to be used as a steam source, the fly ash is also made into industrial bricks, and the oily sludge is recycled; the incinerator capacity per unit area was 0.75 t/(m)2× h) which is 1.4 times of that of an atmospheric fluidized bed incinerator, the carbon content of fly ash is about 0.65 percent, the carbon content of fly ash is about 0.85 percent lower than that of fly ash produced by technologies such as an atmospheric fluidized bed and the like, the combustion efficiency is high, the carbon conversion rate is about 96 percent, the carbon conversion rate is about 2 percent higher than that of other technologies, the yield of saturated steam is 3.6 t (steam)/t (oily sludge), the energy recovery rate can reach 90 percent, the energy recovery rate is equivalent to that of the traditional technology, the discharge amount of nitrogen oxide in produced flue gas is 800 ppm and about 20 percent lower than that of the traditional technology, after the flue gas is treated by a medium-temperature and wet flue gas denitration and dust removal integrated system, the content of nitrogen oxide is 40 ppm and is lower than 50 ppm of national nitrogen oxide discharge standard, namely, the.
Example 2
In the embodiment, oil field oily sludge with high heat value is used as a raw material, the water content is 70%, the heat value is 3000 kcal/kg, and the sludge treatment capacity is 5t/h, so that the fuel supply system 7, the first combustor 8 and the second combustor 9 are not contained in the embodiment 2, and the combination of the two combustors is shown in figures 3 and 4:
the incineration process of the oily sludge is as follows:
1) loading an oily sludge raw material A from an oily sludge source into a sludge receiving system 2, and then transporting the oily sludge raw material A to a sludge storage system 3 for storage and standby, wherein in the receiving and storage processes, odor B volatilized from the sludge receiving system 2 and the sludge storage system 3 is collected by an odor collecting/pressurizing system 4 and discharged from the odor collecting/pressurizing system 4, and the discharged odor B enters an incinerator 1 for incineration (after the incinerator is started);
2) 20000 Nm generated by pressurized combustion air supply system 53The 25 ℃ and 0.5 MPa pressurized air C enters the pressurized combustion air preheating system 6, exchanges heat with the high-temperature pressurized wet flue gas G with the nitrogen oxide content of 800 ppm, the temperature of 900 ℃ and 0.5 MPa from the fluidized bed incinerator (called incinerator for short) 1, is heated into the high-temperature pressurized air D with the temperature of 200 ℃ and 0.5 MPa, and is discharged from the pressurized combustion air preheating system 6; meanwhile, the high-temperature pressurized wet flue gas H is cooled to the middle-temperature pressurized wet flue gas P with the temperature of 750 ℃, the pressure of 0.5 MPa and the content of nitric oxides of 720 ppm and is discharged from the pressurized combustion air preheating system 6;
3) high-temperature pressurized air D discharged from the pressurized combustion air preheating system 6 is totally introduced into the incinerator 1 as main combustion air E, and under the pneumatic action of the main combustion air E, the fluidizing medium in the incinerator 1 is in a fluidizing state at the temperature of 900 ℃;
4) supplying oil-containing sludge F with volatilized odor from an oil sludge storage system 2 into an incinerator 1 at a feeding rate of 5t/h while introducing main combustion air E into the incinerator 1, wherein the oil-containing sludge F with volatilized odor enters the incinerator 1 to be mixed with gas F, then carrying out combustion reaction at high temperature to generate high-temperature pressurized wet flue gas G with the temperature of 900 ℃, the pressure of 0.5 MPa and the content of nitrogen oxides of 800 ppm, and discharging the high-temperature pressurized wet flue gas G from the incinerator 1;
5) the high-temperature pressurized wet flue gas G with the nitrogen oxide content of 800 ppm and the temperature of 900 ℃ and the pressure of 0.5 MPa discharged from the incinerator 1 enters a pressurized combustion air preheating system 6 to exchange heat with low-temperature pressurized air C, is cooled to medium-temperature pressurized wet flue gas P with the nitrogen oxide content of 720 ppm and the medium-temperature pressurized wet flue gas P is discharged from the pressurized combustion air preheating system 6, wherein the medium-temperature pressurized wet flue gas P has the temperature of 750 ℃ and the pressure of 0.5 MPa;
6) the medium temperature pressurized wet flue gas P discharged from the pressurized combustion air preheating system 6 enters the medium temperature wet flue gas denitration and dust removal integrated system 10, is subjected to purification treatment such as denitration and dust removal to form medium temperature pressurized clean flue gas Q with the nitrogen oxide content of 40 ppm at 750 ℃, 0.5 MPa and the like, and is discharged from the medium temperature wet flue gas denitration and dust removal integrated system 10, and meanwhile, fly ash R with the carbon content of 0.5 percent at 0.25t/h removed from the flue gas is also discharged from the medium temperature wet flue gas denitration and dust removal integrated system 10;
5) the medium-temperature pressurized clean flue gas Q discharged from the medium-temperature and wet flue gas denitration and dust removal integrated system 10 enters a waste heat recovery system 11, heat exchange is carried out between a cooling medium and the medium-temperature pressurized clean flue gas Q, the medium-temperature pressurized clean flue gas Q is cooled to be 250 ℃ and 0.5 MPa, the low-temperature pressurized clean wet flue gas S is pressurized to recover waste heat, 15 t/h of 160 ℃ and 0.6 MPa of saturated steam is generated to be used as a steam source, and the low-temperature pressurized clean wet flue gas S is discharged from the waste heat recovery system 11 after heat exchange;
5) the low-temperature pressurized clean wet flue gas S discharged from the waste heat recovery system 11 enters the flue gas pressure reduction system 12 to be reduced into low-temperature normal-pressure clean wet flue gas T and is discharged from the flue gas pressure reduction system 12;
5) the pressure of the flue gas discharged from the flue gas pressure reduction system 12 is reduced into low-temperature normal-pressure clean wet flue gas T which enters the flue gas humidity reduction system 13, and the low-temperature normal-pressure clean dry flue gas U is subjected to humidity reduction treatment and discharged from the flue gas humidity reduction system 13;
5) the low-temperature normal-pressure clean dry flue gas U discharged from the flue gas dehumidification system 13 enters the flue gas discharge system 14 to be discharged after reaching the standard;
5) the fly ash S discharged from the medium-temperature and wet flue gas denitration and dust removal integrated system 10 enters the fly ash discharge tank storage system 15 for storage, and is discharged and added into the fly ash resource utilization system 16 for resource utilization after being accumulated in a sufficient amount.
Through the embodiment, the oily sludge is subjected to incineration treatment, the oily sludge is changed into smoke and fly ash after the incineration, and the residual residue after the treatment is 0.25t/h, so that the amount of solid waste is reduced to 5% of the original amount, and the reduction treatment is realized; meanwhile, the flue gas is purified and discharged up to the standard, and basically has no pollution to the environment, and the fly ash is manufacturedThe industrial brick does not pollute the environment, and realizes the harmless treatment of the oily sludge; the waste heat generated after the oily sludge is burnt is converted into saturated steam to be used as a steam source, the fly ash is also made into industrial bricks, and the oily sludge is recycled; the incinerator has a treatment capacity per unit area of 2 t/(m)2× h) which is 2.16 times that of an atmospheric fluidized bed incinerator, the carbon content of fly ash is about 0.5 percent, the carbon content of fly ash is about 1 percent lower than that of fly ash produced by technologies such as an atmospheric fluidized bed and the like, the combustion efficiency is high, the carbon conversion rate is higher than 99 percent, the carbon conversion rate is about 5 percent higher than that of other technologies, the yield of saturated steam is 31 t (heating water)/t (oil-containing sludge) (containing heat of supplementary fuel, the supplementary heat is about 10 percent), the energy recovery rate can reach 88 percent, the emission rate is equivalent to that of the traditional technology, the emission amount of nitrogen oxide in produced flue gas is 800 ppm, the emission rate is about 18 percent lower than that of the traditional technology, after being treated by a medium-temperature and humidity flue gas denitration and dust removal integrated system, the content of nitrogen oxide is 200 ppm, and the emission standard of the national nitrogen oxide is lower than.
In addition, in example 2, the pressure is higher and the processing capacity, processing effect, and the like are better than those in example 1, but mechanical energy consumption (electric energy) for air supply may be increased to some extent, increasing electric energy consumption.
Claims (5)
1. The utility model provides a pressurized fluidized bed oily sludge incineration system, including burning furnace (1), fatlute receiving system (2), fatlute jar stores up system (3), odor is collected/pressurization system (4), pressurization combustion air supply system (5), pressurization combustion air preheats system (6), fuel supply system (7), first combustor (8), second combustor (9), medium temperature and humidity flue gas denitration dust removal integrated system (10), waste heat recovery system (11), flue gas pressure reduction system (12), flue gas dehumidification system (13), flue gas discharge system (14), flying dust discharge tank storage system (15) and flying dust utilization system (16), its characterized in that:
the incinerator (1) is provided with a main combustion air inlet (1-1), an oily sludge inlet (1-2) of the incinerator, a first flue gas inlet (1-3), a second flue gas inlet (1-4), an odor inlet (1-5) and a high-temperature pressurized wet flue gas outlet (1-6), wherein the main combustion air inlet (1-1) is communicated with the high-temperature pressurized air outlet (6-3) of the pressurized combustion air preheating system (6), a fuel outlet (7-1) of the fuel supply system (7), a mixed combustion matter inlet (8-1) of the first combustor (8) and a mixed combustion matter inlet (9-1) of the second combustor (9); an oily sludge inlet (1-2) of the incinerator is communicated with a second oily sludge outlet (2-4) of the oil sludge receiving system (2) and an oily sludge outlet (3-3) of the oil sludge storage system (3); the first flue gas inlet (1-3) is communicated with a flue gas outlet (8-2) of the first combustor (8); the second flue gas inlet (1-4) is communicated with a flue gas outlet (9-2) of the second combustor (9); the odor inlet (1-5) is communicated with the odor outlet (4-3) of the odor collecting/pressurizing system (4); the high-temperature pressurized wet flue gas outlet (1-6) is communicated with a high-temperature pressurized wet flue gas inlet (6-2) of the pressurized combustion air preheating system (6);
the oily sludge receiving system (2) is provided with an oily sludge inlet (2-1), a first oily sludge outlet (2-2), an odor outlet (2-3) and a second oily sludge outlet (2-4), wherein an oily sludge inlet (2-1) of the oil sludge receiving system is communicated with an oily sludge source, a first oily sludge outlet (2-2) is communicated with an oily sludge inlet (3-1) of the oil sludge storage system (3), an odor outlet (2-3) of the oil sludge receiving system is communicated with a first odor inlet (4-1) of an odor collecting/pressurizing system (4), and a second oily sludge outlet (2-4) is communicated with an oily sludge outlet (3-3) of the oil sludge storage system (3);
the oil sludge storage system (3) is provided with an oily sludge inlet (3-1) of the oil sludge storage system, an odor outlet (3-2) of the oil sludge storage system and an oily sludge outlet (3-3), and the odor outlet (3-2) of the oil sludge storage system is communicated with a second odor inlet (4-2) of the odor collecting/pressurizing system (4);
the pressurized combustion air preheating system (6) is provided with a low-temperature pressurized air inlet (6-1), a high-temperature pressurized wet flue gas inlet (6-2), a high-temperature pressurized air outlet (6-3) and a warm pressurized wet flue gas outlet (6-4), wherein the low-temperature pressurized air inlet (6-1) is communicated with the low-temperature pressurized air outlet (5-1) of the pressurized combustion air supply system (5), and the warm pressurized wet flue gas outlet (6-4) is communicated with a medium-temperature pressurized clean wet flue gas inlet (10-1) of the medium-temperature wet flue gas denitration and dust removal integrated system (10);
the fuel outlet (7-1) of the fuel supply system (7) is communicated with the mixed combustion material inlet (8-1) of the first combustor (8) and the mixed combustion material inlet (9-1) of the second combustor (9);
the medium-temperature wet flue gas denitration and dust removal integrated system (10) is provided with a medium-temperature pressurized clean wet flue gas inlet (10-1), a medium-temperature pressurized clean flue gas outlet (10-2) and a fly ash outlet (10-3), wherein the medium-temperature pressurized clean flue gas outlet (10-2) is communicated with the medium-temperature pressurized clean flue gas inlet (11-1) of the waste heat recovery system (11); the fly ash outlet (10-3) is communicated with a fly ash inlet (15-1) of a fly ash discharge tank storage system (15);
a fly ash outlet (15-2) of the fly ash discharge tank storage system (15) is communicated with a fly ash inlet (16-1) of a fly ash resource utilization system (16);
the low-temperature pressurized clean wet flue gas outlet (11-2) of the waste heat recovery system (11) is communicated with the low-temperature pressurized clean wet flue gas inlet (12-1) of the flue gas pressure reduction system (12);
a low-temperature normal-pressure clean wet flue gas outlet (12-2) of the flue gas pressure reduction system (12) and a low-temperature normal-pressure clean wet flue gas inlet (13-1) of the flue gas dehumidification system (13);
the low-temperature normal-pressure clean dry flue gas outlet (13-2) of the flue gas dehumidification system (13) is communicated with the low-temperature normal-pressure clean dry flue gas inlet (14-1) of the flue gas discharge system (14).
2. A pressurized fluidized bed oily sludge incineration system according to claim 1, characterized in that said incinerator (1) is a pressurized fluidized bed incinerator, employing a pressurized bubbling fluidized bed reactor.
3. A pressurised fluidized bed oily sludge incineration system according to claim 1, characterised in that the fuel supply system (7) is oil or gas.
4. A pressurized fluidized bed oily sludge incineration system according to claim 1, characterized in that the charging opening of said incinerator (1) can be located in the dilute phase zone of the upper part of the furnace or in the dense phase zone of the lower part of the furnace.
5. The pressurized fluidized bed oily sludge incineration system according to claim 1, characterized in that the medium temperature wet flue gas denitration and dust removal integrated system (10) is a high temperature integrated system.
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| CN110375310B (en) * | 2019-07-08 | 2024-03-08 | 陕西正本环境工程有限公司 | Pressurized fluidized bed oil-containing sludge incineration system and incineration treatment method thereof |
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