CN210345490U - Incineration disposal system for organic chemical fine distillation residues - Google Patents

Abstract

The utility model provides an organic chemical industry fine distillation residue burns processing system, belong to environmental protection and energy saving and discarded object utilization technical field, the one end of residue incinerator forms integral type U type structure after with the fixed intercommunication of exhaust-heat boiler, exhaust-heat boiler's right side wall and cyclone intercommunication, U type flue and quench tower top intercommunication are passed through to cyclone's top, the import intercommunication of venturi and bag collector is passed through to the right side wall of quench tower, the import intercommunication of pipeline and deacidification tower is passed through in bag collector's export, pipeline and flue gas reheater intercommunication are passed through on the top of deacidification tower, flue gas reheater's lower extreme and SCR denitrification facility intercommunication, pipeline and draught fan and chimney intercommunication are passed through in SCR denitrification facility's export. The system gives consideration to ecological benefits and economic benefits, has thorough treatment effect on three wastes in the chemical industry, has no secondary pollution, and has compact overall layout, small occupied area and strong continuous working capacity.

Description

Incineration disposal system for organic chemical fine distillation residues

Technical Field

The invention belongs to the technical field of environmental protection, energy conservation and waste resource utilization, and particularly relates to an organic chemical engineering fine distillation residue incineration disposal system.

Background

The organic chemical industry comprises basic organic chemical industry, high-molecular chemical industry and fine chemical industry. The organic chemical industry is a typical heavy pollution industry, products, intermediate products and raw materials of the organic chemical industry are dangerous chemicals, and distillation residues of the organic chemical industry are more environmental problems of various pollutants, large discharge amount, complex components, serious environmental pollution and the like. At present, the management of industrial solid wastes in China lags behind the management of waste gases and waste water as a whole. The method adopts a whole-process management mode, and relevant national standards of identification, treatment and disposal of hazardous wastes are issued successively; however, the comprehensive utilization of the hazardous wastes is still vacant in management, and particularly, the comprehensive utilization of the hazardous wastes is problematic in secondary pollution supervision.

The organic chemical rectification (distillation) residue is mostly dangerous waste, the treatment and disposal of the organic chemical rectification (distillation) residue also follow three principles of reclamation, reduction and harmlessness of solid waste treatment and disposal, the treatment and disposal modes mainly comprise four modes, namely comprehensive utilization, incineration, landfill and sewage treatment, the ways are divided into an on-site mode and an off-site mode, and the final result of the disposal is to eliminate various dangers of the rectification (distillation) residue. The main problems existing in the prior rectification residue pretreatment are dehydration and solidification of the rectification residue. The method for dehydrating the rectification residue is mainly used in stacking yards for producing enterprises or treating enterprises, has the problems that organic matters are volatilized into the air and the generated leachate is treated, pollutants generated by the organic matters volatilized into the air basically have no enterprise attention, and some enterprises collect the leachate to treat the leachate and some enterprises are equivalent to natural air drying. Part of the distillation residue is not only organic components but also catalyst or reactant, and the like, and part of the distillation residue contains heavy metal or more than one, and at present, most of the treatment methods adopted are incineration treatment and landfill. Because a plurality of organic matters are incinerated together during incineration, the incinerated components have dilution effect, so that generally, no curing measure is adopted, and a part of dangerous waste needing curing is not cured.

At present, because the technological level of China is rough, few enterprises are available for carrying out secondary rectification treatment on rectification (distillation) residues. Although the state clearly shows that the unit which does not obtain the hazardous waste operation license can not engage in the hazardous waste operation activity and seriously attacks the behaviors of illegally transferring and disposing the rectification residue, many enterprises still sell the residue to the enterprises which do not have qualified units for disposal. The subsequent destination of the residue is lack of supervision and data are not clear, so that the environmental pollution risk is extremely high; meanwhile, the residue after secondary rectification can also generate more waste water, waste gas, rectification (distillation) residue and other wastes, and the risk of environmental pollution caused by management deficiency is very high.

Some distillation residues are flammable and have high fuel value, and are used as fuel inside and outside enterprises, and in the investigation process, the boilers are found to be part of the enterprise production process, only meet the requirements of the enterprise production, and whether the requirements of hazardous waste incineration are met is unknown, so that the risk of the part of distillation residues on environmental damage can be increased.

If leakage occurs during storage and transportation of the distillation residue, soil, underground water and surface water are inevitably polluted, even atmospheric ozone is possibly destroyed, and the atmospheric environment around a treatment facility is easily polluted secondarily by common distillation residue treatment technologies such as secondary distillation incineration and the like. Therefore, comprehensive utilization, treatment technology and management system of the residues need to be planned from the aspects of strong control sources, local utilization and the like.

The residues produced in the rectification (distillation) production process are different due to different raw materials, different processes and different equipment in chemical production. Therefore, the distillation residue has various components and is very difficult to qualitatively and quantitatively analyze and detect. The distillation residue is usually sticky and solid, some of which are in liquid state, and the components mainly comprise asphalt residue, tar residue, waste acid tar, phenol residue, toluene residue, liquefied petroleum gas residual liquid (containing benzopyrene, chrysene, naphthalene, fluoranthene and polycyclic aromatic hydrocarbon waste) and the like. For example: the distillation residue of methanol contains dimethylpentane, butanol, pentanol, hexanol, higher alcohols, etc.; the rectification residue of vinyl chloride contains vinyl chloride, dichloroethane, dichloroethylene, trichloroethane, trichloroethylene, etc.; about 0.6 ton of acetone by-product was produced in the phenol production process and finally entered the phenol purification residue. That is, the distillation residue contains both the feed and the product as well as further intermediate components. Common methods for treating distillation residues include physical methods, biological methods, wet oxidation methods, incineration methods, and the like. Physical methods, biological methods and wet oxidation methods all have certain defects of imperfect treatment.

The incineration method is economical for disposing the rectification (distillation) residues, and the incineration process is a comprehensive reaction process integrating multiple disciplines such as physical change, chemical change, catalytic reaction, aerodynamics, heat transfer and the like. The incineration method is used for treating rectification (distillation) residues with high concentration, high toxicity and complex components, not only realizes reduction and harmlessness, but also can realize resource utilization of heat generated by incineration.

Disclosure of Invention

The invention aims to provide an organic chemical industry fine distillation residue incineration disposal system, which solves the defects of the prior art in the current domestic market, and aims at the purposes that the fine distillation residue contains less halogen such as chlorine, fluorine and the like, contains other acid radical ions, has more complex smoke components, realizes the full combustion of the organic chemical industry fine distillation residue, thoroughly incinerates the pollution hazard and the great toxicity of the fine distillation residue, and recycles inorganic salt generated by incineration and high-temperature waste heat generated in the incineration process.

The invention relates to an organic chemical industry fine distillation residue incineration disposal system which is realized by the following mode, one end of a residue incinerator is fixedly communicated with a waste heat boiler to form an integrated U-shaped structure, in view of reducing consumption of auxiliary fuel as much as possible, the main incinerator part of the residue incinerator adopts a heat insulation incinerator, the furnace wall of the heat insulation incinerator adopts compact corundum or chrome corundum refractory castable or refractory brick with acid and alkali corrosion resistance on the fire surface, the structure is compact, the heat loss is little, the other end and the bottom of the residue incinerator is the heat insulation incinerator, the residue incinerator can be divided into three parts of the top part, the upper part and the lower part according to the structure, wherein the top part is provided with a residue atomization spray gun, the residue atomization spray gun adopts an internal mixing type steam atomization spray gun, and steam produced by the boiler is used for atomizing residue. Four main burners connected with a combustion fan, an organic waste gas booster fan and a natural gas pipeline are arranged at the same cross section of two side walls of a furnace wall at corresponding positions along the height direction of the residue incinerator, and the flame of the four main burners forms a tangential combustion state with the center of the hearth as the center of a circle and the radius of about 300-500mm at the cross section of the hearth, so that the disturbance and the residence time of the flame in the hearth are increased, and the main combustion area is ensured to burn off organic matters in the atomized residues. The afterburning burner is installed at the corresponding position of the U-shaped channel at the lower part of the heat insulation incinerator, and aims to further heat up inorganic salt in the fine distillation residues to enable the inorganic salt to reach a molten flowing state, so that the inorganic salt can conveniently flow out of the incinerator, and simultaneously, residual organic matters in the inorganic salt can be further incinerated and burned out, so that the inorganic salt flowing out of the incinerator is ensured to reach the industrial salt level standard for cyclic utilization, and the situation that the inorganic salt flowing out of the incinerator is still dangerous waste due to residual organic matters is avoided, and further treatment or landfill is needed according to the dangerous waste requirement, and secondary disposal waste of enterprises is caused. Have arranged along the corresponding position of residue incinerator four sides furnace wall and have beaten the hole, beat and set up two round holes on the hole device of coking, the observation hole of one of them for adopting heat-resisting glass to constitute, beat the hole device upper portion of coking in arranging, can observe burning situation and the stove wall salt deposit condition in the stove, can adopt the drill rod of coking to beat the coking to the stove wall salt deposit position through the hole of beating coking device lower part round hole in view of the above, make the salt deposit bottom the residue incinerator of U type structure, the hole of beating coking device lower part round hole utilizes the door of beating coking that sets up to make it be in the closed condition when not beating the coking, ensure not to furnace hourglass wind.

The other side of the residue incinerator is provided with a waste heat boiler, a steam pocket of the waste heat boiler is independently arranged at a certain position on the upper part of the waste heat boiler, four boiler walls of the waste heat boiler are enclosed by membrane water-cooling walls, and an upper collecting box and a lower collecting box of the membrane water-cooling walls, the steam pocket, an additional downcomer arranged independently and an additional steam-water ascending pipe arranged independently form an additional closed circulation loop; the waste heat boiler is internally provided with a plurality of groups of L-shaped quenching screen type heating surfaces, a steam-water outlet pipe of a header at the top ends of the L-shaped quenching screen type heating surfaces is communicated with the steam pocket, and the internally arranged L-shaped quenching screen type heating surfaces, the steam pocket, the independently arranged centralized downcomer and the independently arranged steam-water riser form a closed circulation loop. The waste heat boiler in the form of the membrane type water wall furnace wall and the arrangement of a plurality of groups of L-shaped membrane type wall quenching screen type heating surfaces arranged in the waste heat boiler can instantly reduce the salt-containing high-temperature flue gas at 1100 ℃ to below 550 ℃ on one hand, so that inorganic salt in a molten state is instantly converted from a liquid state or a gaseous state into a solid state, part of solid salt is deposited at the bottom of the U-shaped incinerator by virtue of gravity, the high-temperature flue gas, the salt liquid in the molten state and the afterburning burner are reheated to enable the solid salt to flow out of the incinerator, and solid fine salt particles taken away by the flue gas can be recovered in a rear-stage device. And a steam soot blowing device or a gas pulse soot blowing device is arranged at the corresponding position of the waste heat boiler, and inorganic salt adhered to the waste heat boiler and a plurality of groups of L-shaped film type wall quenching screen type heating surfaces arranged in the waste heat boiler is cleaned on line and deposited at the bottom of the U-shaped structure incinerator.

The flue gas outlet of the waste heat boiler is communicated with the cyclone separator, the flue gas containing solid fine salt particles is subjected to further gas-solid separation through the cyclone separator, the solid fine salt particles in the flue gas are separated and enter the replacement bin a arranged at the lower part of the cyclone separator, the solid fine salt particles collected in the replacement bin a are washed through nitrogen, so that corrosive components in the flue gas doped in the solid fine salt particles are separated, the gas subjected to nitrogen replacement separation is sent into the alkaline tower, and inorganic salt without corrosive components can be sent into the water-cooled scraper plate through the star-shaped discharge valve to be conveyed and recycled in a centralized manner. In order to avoid corrosive gas corroding devices behind the lower part of the cyclone separator, a star-shaped discharge valve is arranged between the cyclone separator and the replacement bin a. The replacement bin a adopts steam for heat mixing, so that the temperature of the replacement bin a is prevented from being kept above 30 ℃ of acid dew point temperature, and the replacement bin a is ensured not to be corroded and can normally work.

The flue gas with the temperature of 500-. The solid fine salt particles recovered in the lower replacement bin b of the quenching tower are also replaced by nitrogen in the same manner as in the lower replacement bin a of the cyclone. In order to avoid the corrosion of corrosive gas to the device behind the lower part of the water spray cooling quench tower, a star-shaped discharge valve is arranged between the quench tower and the replacement bin b. The replacement bin b adopts steam for heat mixing, so that the temperature of the replacement bin is not prevented from being kept above 30 ℃ of the acid dew point temperature, and the replacement bin is ensured not to be corroded and can normally work.

A venturi tube is arranged on a flue between the quenching tower and the bag type dust collector, an active carbon injection device and a quick lime injection device are arranged on the venturi tube, and the second factor in the smoke is further adsorbed and desorbed.

The outlet flue gas of quench tower connects gradually venturi, bag collector through the flue, bag collector adopts online pulse to blow grey, the upper end of bag collector is provided with the compressed air buffer tank, compressed air utilizes exhaust-heat boiler self-produced steam to adopt vapour gas heat exchanger to heat it to about 120 ℃, the bag collector lower extreme is provided with the ash bucket, steam heat tracing pipeline has been arranged to the ash bucket outer wall, it is above 30 ℃ to guarantee to keep in the ash bucket at acid dew point temperature, prevent that ash bucket outer wall temperature is less than acid dew point temperature.

The outlet flue gas of the bag type dust collector is communicated with a deacidification tower through a pipeline, a multistage circulating spray washing pipe, a multistage cyclone separator, a multistage flue gas uniform distributor and a multistage packing layer are arranged in the deacidification tower, a demister consisting of baffle plates or silk screens is installed at the top of the deacidification tower, the outlet at the lower end of the deacidification tower is communicated with a three-stage or multistage sedimentation tank for deacidification liquid, and the sedimentation tank is supplemented with alkali liquor for adjustment according to the pH value of the deacidification liquid in a tank at the lower part of the deacidification tower. The deacidification tower adopts a mode of countercurrent spraying with the flow direction of the flue gas, an alkali liquor spraying and washing pipe is arranged on the upper part of a flue gas packing layer of each stage to carry out neutralization washing on the flue gas, deacidification liquid after deacidification of the flue gas is deposited in a lower end storage tank of the deacidification tower by means of gravity, and the lower part of the lower end storage tank of the sulfur tower is communicated to a deacidification liquid sedimentation tank through a pipeline and a valve so as to discharge deacidification sewage. The deacidification liquid sedimentation tank is connected and adjacent to the neutralization tank and the clean water tank by an overflow structure, and alkali liquor is supplemented to the neutralization tank at regular time according to the change of the pH value of the deacidification liquid in a storage tank at the lower end of the deacidification tower.

The flue gas at about 50 ℃ from the deacidification tower is communicated with a flue gas reheater through a pipeline, and the flue gas is burnt by natural gas in the flue gas reheater through a burner to raise the temperature of the flue gas at about 50 ℃ to about 220 ℃. A certain part of the lower end of the flue gas reheater is provided with 2-3 layers of SCR denitration catalyst modules, and an atomized ammonia spraying port and an even air pore plate are arranged between the flue gas reheater and the denitration catalyst modules. The SCR denitration device selects a medium-low temperature catalyst, the operation temperature is between 160 ℃ and 240 ℃, the sprayed ammonia water and the SCR denitration catalyst can be used for reducing nitrogen oxides generated in the residue burning process, NOx is converted into N2 and H2O, the denitrated flue gas can be connected with an induced draft fan through a flue, and clean flue gas is introduced into a chimney through the induced draft fan and is exhausted.

The lower end of the residue incinerator is communicated with the double-shaft cooler through the expansion joint, the outlet of the double-shaft cooler is communicated with the inlet of the water-cooling scraper slag remover, the salt discharging mode at the lower part of the residue incinerator is molten liquid salt discharging, and the molten salt at 1100 ℃ enters the water-cooling scraper slag remover after entering the double-shaft cooler for cooling, so that solid salt collection can be realized. The water-cooled scraper slag remover is conveyed to a burning salt storage warehouse, and solid salt collected after burning can be packed, stacked and recycled in the salt storage warehouse; the replacement bin a and the replacement bin b are communicated with the inlet of the water-cooling scraper slag remover through a star-shaped discharge valve and a pipeline through solid-state fine salt after nitrogen replacement, and the outlet of the water-cooling scraper slag remover is communicated with an incineration residue warehouse.

The displacement bin a (16) and the displacement bin b (17) are respectively provided with a displacement nitrogen inlet (38), a safety valve (39) and a displacement nitrogen outlet (40), and the displacement nitrogen outlet (40) is connected to a flue gas inlet at the lower part of the deacidification tower (20) through a pipeline.

The residue atomizing spray gun is communicated with the residue buffer tank through a booster pump and a pipeline, the atomizing agent of the residue atomizing spray gun adopts saturated or superheated steam or compressed air, and the outer wall of the residue buffer tank adopts steam heat tracing to ensure the temperature required by the liquid flow of the residue in the residue buffer tank; the main burner and the afterburning burner are respectively communicated with an external natural gas pipeline, so that external energy required by residue incineration is ensured.

The inner wall of the residue incinerator is preferably coated with an acid and alkali corrosion resistant chromium steel jade refractory castable, and a heat insulation castable is arranged between the inner wall of the residue incinerator and the chromium steel jade refractory castable.

And a demister is arranged in a pipeline communicated with the flue gas reheater.

The waste liquid incinerator and waste heat boiler U-shaped integrated structure is adopted, the layout is compact, the waste heat boiler recovers most of waste heat, and a large amount of fuel cost is saved; the recovered salt is in a liquid salt discharging form and a solid salt collecting form, so that impurities can be effectively removed, and the purity of the salt is high; because the system contains chlorine, in order to control the generation of dioxin harmful substances, the system is provided with a quench tower to rapidly cool the flue gas to the optimum temperature point for skipping the generation of the dioxin harmful substances. In addition, a venturi tube is arranged after quenching, and the metered activated carbon and quicklime powder are sprayed into a flue through a spray fan to be mixed with flue gas, so that heavy metals in the flue gas are absorbed and the generation of dioxin harmful substances is further restrained; in order to prevent the hydrogen chloride from generating dew point corrosion, on one hand, a nitrogen replacement bin is arranged at the lower parts of the cyclone separator and the quench tower to effectively remove hydrogen chloride gas, and on the other hand, the back blowing gas of the bag-type dust remover is heated, and an ash bucket carries out heat tracing to prevent the subsequent equipment from generating dew point corrosion; the incineration system can continuously and effectively treat the high-concentration salt-containing and chlorine-containing organic waste liquid all year round; and finally, the flue gas in the system is subjected to purification treatment by a bag type dust collector, a quick lime and active carbon injection device, a deacidification tower and an SCR denitration device, and is completely discharged after reaching the environmental protection standard. The system gives consideration to ecological benefits and economic benefits, has thorough treatment effect on three wastes in the chemical industry, has no secondary pollution, and has compact overall layout, small occupied area and strong continuous working capacity.

Drawings

FIG. 1 is an overall structural view;

FIG. 2 is a view showing the construction of a waste liquid incinerator;

FIG. 3 is a schematic diagram of a dual shaft cooler;

FIG. 4 is a partial enlarged view;

FIG. 5 is a view of a replacement bin configuration;

as shown in fig. 1 to 5, a combustion fan (1), a water-cooled scraper slag remover (2), a double-shaft cooler (3), an expansion joint (4), a afterburning burner (5), a residue incinerator (6), a chrome corundum refractory castable (7), a heat preservation castable (8), a main burner (9), a residue atomizing spray gun (10), a waste heat boiler (11), a steam drum (12), a cyclone separator (13), a U-shaped flue (14), a water-spraying cooling quench tower (15), a replacement bin a (16), a replacement bin b (17), a venturi tube (18), a bag type dust remover (19), a deacidification tower (20), a demister (21), a burner (22), a flue gas reheater (23), an SCR denitration device (24), an induced draft fan (25), a chimney (26), an organic waste gas booster fan (27), a star-type discharge valve (28), an L-shaped membrane wall quench screen type heating surface (29), a replacement nitrogen inlet (30), a safety valve (31), a replacement nitrogen outlet (32) and a solid waste seeding device (33).

Detailed Description

The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only preferred embodiments of the present invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.

Example 1: the utility model provides an organic chemical industry fine distillation residue burns processing system, the main equipment includes combustion fan 1, water-cooling scraper blade slagging-off machine 2, double-shaft cooler 3, residue burns burning furnace 6, exhaust-heat boiler 11, steam pocket 12, cyclone 13, water spray cooling quench tower 15, bag collector 19, deacidification tower 20, flue gas reheater 23, SCR denitrification facility 24, draught fan 25, chimney 26. The inner wall of the residue incinerator 6 is coated with acid-base corrosion-resistant high-temperature-resistant chromium steel jade refractory castable 7, heat-insulating castable 8 is arranged between the inner wall of the residue incinerator 6 and the chromium steel jade refractory castable 7, and the residue incinerator is provided with a solid waste spreading device 33. The left end of the residue incinerator 6 is divided into a top part, an upper part and a lower part, the top part is provided with a waste liquid atomization spray gun 10, an internal mixing type steam atomization spray gun is selected, four main burners 9 connected with a combustion fan 1, an organic waste gas booster fan 27 and a natural gas pipeline are arranged on the upper part and the middle upper part, the disturbance and the residence time of flame in a hearth are increased, and the main combustion area is ensured to burn off organic matters in atomized residues. The lower part is provided with a afterburning burner 5 connected with the combustion fan 1 and a natural gas pipeline; have arranged along the corresponding position of residue incinerator four sides furnace wall and have beaten the hole, beat and set up two round holes on the hole device of coking, the observation hole that one of them is constituteed for adopting heat-resisting glass, arrange in the hole device upper portion of coking, can observe burning situation and the stove wall salt deposit condition in the stove, can adopt the drill rod of coking to beat the coking to the stove wall salt deposit position through the hole of beating coking device lower part round hole in view of the above, make the salt deposit burn burning furnace bottom to U type structure, the hole of beating coking device lower part round hole utilizes the hole door of beating coking that sets up to make it be in the closed condition when not beating the coking, ensure not to leak out to furnace. The lower end of the residue incinerator 6 is communicated with the double-shaft cooler 3 through the expansion joint 4, the outlet of the double-shaft cooler 3 is communicated with the inlet of the water-cooling scraper slag remover 2 to further cool and collect ash, the right end of the waste liquid incinerator 6 is fixedly communicated with the waste heat boiler 11 to form an integrated U-shaped structure, and the structure is compact and has less heat loss. The waste heat boiler 11 adopts a vertical membrane type water-cooled wall structure, a plurality of groups of L-shaped quenching screen type heating surfaces 29 are arranged in the waste heat boiler, the top of the waste heat boiler is connected with a steam pocket 12, the side wall of the waste heat boiler is communicated with a cyclone separator 13, the top end of the cyclone separator 13 is communicated with the top end of a water spray cooling quenching tower 15 through a U-shaped flue 14, the right side wall of the water spray cooling quenching tower 15 is communicated with the inlet of a bag type dust collector 19 through a Venturi tube 18, the outlet of the bag type dust collector 19 is communicated with the inlet of a deacidification tower 20 through a pipeline, part of salts of the cyclone separator 13 are collected under the action of centrifugal force and enter a replacement bin a16 at the lower part of the cyclone separator 13 through a star-shaped discharge valve 28, two quenching atomization spray guns are arranged at the shoulder part of the water spray cooling quenching tower 15. The replacement bin a16 and the replacement bin b17 are respectively communicated with an inlet of the water-cooling scraper slag remover 2, and an outlet of the water-cooling scraper slag remover 2 is communicated with an incineration residue warehouse. The venturi tube 18 is provided with a quicklime injection device interface and an active carbon injection device interface which are connected with the quicklime injection device and the active carbon injection device; a bag type dust collector 19 is arranged behind the Venturi tube 18, a compressed air buffer tank is arranged above the bag type dust collector 19, air is preheated to about 120 ℃, an off-line pulse soot blowing mode is adopted, and a soot hopper is arranged below the bag type dust collector 19. The replacement bin a16 and the replacement bin b17 are respectively provided with a replacement nitrogen inlet 38, a safety valve 39 and a replacement nitrogen outlet 40, and the replacement nitrogen outlet 40 is connected to a flue gas inlet at the lower part of the deacidification tower 20 through a pipeline. An alkali liquor nozzle and a demister 21 are arranged at the top of the deacidification tower 20, and a flue gas reheater 23 is arranged behind the deacidification tower 20. The flue gas reheater 23 is arranged with a flue gas reheating burner 22; an SCR denitration device 24 is arranged behind the flue gas reheater 23; and an ammonia spraying grid is arranged in the inlet flue of the SCR denitration device 24. The flue gas reaching the requirements of the national environmental protection standard is sent into a chimney 26 by an induced draft fan 25.

The specific working process is as follows: after equipment, fuel readiness, at first the air passes through combustion fan 1, organic waste gas booster fan and natural gas and carries main burner 9 in the incinerator together, opens the draught fan 25, keeps the interior little negative pressure of furnace, starts ignition and ignites, when furnace temperature is close reasonable temperature interval, carries the high concentration salt containing chlorine organic waste liquid to waste liquid atomizing spray gun 10 through the waste liquid booster pump, lets in compressed air, and the waste liquid is atomized and burns in furnace. In the incineration process, the combustion of a afterburning burner 5 at the lower part of a hearth prevents molten salt from cooling and blocking the hearth outlet of the incinerator, ash slag in a molten state continuously falls into a double-shaft cooler 3 below the incinerator, and the ash slag falls into a scraper slag remover 2 below the incinerator after being initially cooled and is further cooled and recovered; the incinerated flue gas enters a waste heat boiler 11, the waste heat boiler 11 utilizes circulating cooling water in a membrane type water-cooling wall to exchange heat with the flue gas to generate saturated steam, the flue gas is rapidly cooled through a cooling chamber, a steam pocket 12 of the waste heat boiler 11 is independently arranged at a certain position on the upper part of the waste heat boiler 11, four boiler walls of the waste heat boiler 11 are enclosed by the membrane type water-cooling wall, and an upper header and a lower header of the membrane type water-cooling wall, the steam pocket 12, an additional downcomer arranged independently and an additional steam-water ascending pipe arranged independently form an additional closed circulation loop; the waste heat boiler 11 is internally provided with a plurality of groups of L-shaped quenching screen type heating surfaces 29, a steam-water outlet pipe of a header at the top end of each L-shaped quenching screen type heating surface 29 is communicated with the steam drum 12, and the L-shaped quenching screen type heating surfaces 29, the steam drum 12, the independently arranged centralized descending pipes and the independently arranged steam-water ascending pipes form a closed circulation loop. The waste heat boiler 11 in the form of the membrane wall furnace wall and the L-shaped membrane wall quenching screen type heating surfaces 29 arranged in the waste heat boiler 11 can instantly reduce the temperature of high-temperature flue gas containing salt at 1100 ℃ to be below 550 ℃ on one hand, inorganic salt in a molten state is instantly converted from a liquid state or a gaseous state to a solid state, part of solid salt deposits the bottom of the residue incinerator 6 with a U-shaped structure by virtue of gravity, the high-temperature flue gas, the salt liquid in the molten state and the afterburning burner 5 reheat the salt liquid so as to flow out of the incinerator, and solid fine salt particles taken away by the flue gas can be recovered in a rear-stage device without having adhesive property. And a steam soot blowing device or a gas pulse soot blowing device is arranged at the corresponding position of the waste heat boiler 6, and inorganic salt adhered to the waste heat boiler 6 and a plurality of groups of L-shaped film type wall quenching screen type heating surfaces 29 arranged in the waste heat boiler 6 is cleaned on line and deposited at the bottom of the residue incinerator 6 with a U-shaped structure. (ii) a The waste heat boiler 11 is connected with a cyclone separator 13 at the back, part of salts are collected under the action of centrifugal force, and then the flue gas with the temperature of 500-. Because the incineration waste liquid contains chlorine, in order to control the generation of dioxin harmful substances, a water spraying cooling quenching tower 15 is arranged to rapidly cool the flue gas from 550 ℃ to 180 ℃, so that the optimal temperature point for generating the dioxin harmful substances is skipped. And a venturi tube 18 is arranged on a flue behind the water spraying cooling quenching tower 15, and the metered activated carbon and quicklime powder are sprayed into the flue through a spraying fan to be mixed with the flue gas, so that heavy metals in the flue gas are absorbed and the generation of dioxin harmful substances is further suppressed. The flue gas after the rapid cooling gets into bag collector 19 that sets up at the back, for preventing that the flue gas cooling from reaching dew point and corroding bag collector 19, this system has taken two measures: firstly, the blowback compressed air is preheated to about 120 ℃; secondly, the ash bucket of the bag-type dust remover is heated to more than 110 ℃. The preheated compressed air carries out off-line pulse soot blowing on the bag-type dust collector 19 from the spray holes on the side wall, and ash content, quicklime and activated carbon powder in the flue gas are collected by the ash hopper which is heated by the heat tracing below and are subjected to centralized processing. Flue gas leaving the bag type dust collector 19 enters a deacidification tower 20, alkali liquor in an alkali liquor tank is sprayed into the tower from an alkali liquor nozzle at the upper part of the deacidification tower 20 by using a circulating spray pump, the alkali liquor and the flue gas are in full contact reaction, residual moisture in the deacidified flue gas is removed by a demister 21 arranged at the top end of the deacidification tower 20 and in a flue gas pipeline later, and wastewater after deacidification reaches a certain water level is discharged to a wastewater treatment plant by a deacidified wastewater leading-out pump; the flue gas from which the residual moisture is removed enters a flue gas reheater 23, natural gas is introduced into the flue gas reheating burner 22, and the flue gas reaching about 220 ℃ through the flue gas reheater 23 enters a next stage of tail gas treatment equipment SCR denitration device 24. The flue gas enters the denitration system, is firstly mixed with the sprayed urea solution, and can be uniformly distributed in the flue gas for the sprayed urea solution, so that an ammonia spraying grid is arranged in the inlet flue. The mixed flue gas enters an SCR denitration device 24 for NOx removal reaction. The flue gas up to standard after SCR denitrification facility 24 handles is drawn out by draught fan 25. In the induced draft fan 25, the flue gas is further cooled by the circulating cooling water that is set up. The clean flue gas meeting the requirements of the national environmental protection standard is introduced into a chimney 26 through an induced draft fan 25 and is discharged into the atmosphere.

In the present invention, unless otherwise expressly stated or limited, the terms "mounted," "disposed," "connected," "fixed," "connected," and the like are to be construed broadly and can, for example, be fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; the terms may be directly connected or indirectly connected through an intermediate, and may be communication between two elements or interaction relationship between two elements, unless otherwise specifically limited, and the specific meaning of the terms in the present invention will be understood by those skilled in the art according to specific situations.

Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.

Claims (10)

1. The incineration disposal system for the organic chemical refined distillation residues is characterized in that one end of a residue incinerator (6) is fixedly communicated with a waste heat boiler (11) to form an integral U-shaped structure, the other end of the residue incinerator (6) is divided into a top part, an upper part and a lower part, wherein the top part is provided with a residue atomization spray gun (10), two side walls of the upper part of a hearth of the residue incinerator (6) are respectively provided with four main burners (9) connected with a combustion fan (1), an organic waste gas booster fan (27) and a natural gas pipeline, the lower part of the residue incinerator (6) is provided with a afterburning burner (5) connected with the combustion fan (1) and the natural gas pipeline, a plurality of groups of L-shaped membrane wall quenching screen type heating surfaces (29) are arranged in the waste heat boiler (11), a flue gas outlet of the waste heat boiler (11) is communicated with a cyclone separator (13), the top end of the cyclone separator (13) is communicated with the top end of, a flue gas outlet of the water spraying cooling quench tower (15) is connected with a Venturi tube (18) through a flue, the Venturi tube (18) is communicated with a bag type dust collector (19) through the flue, a flue gas outlet of the bag type dust collector (19) is communicated with a flue gas inlet of a deacidification tower (20) through a pipeline, the top end of the deacidification tower (20) is communicated with a flue gas reheater (23) through a pipeline, the lower end of the flue gas reheater (23) is communicated with an SCR denitration device (24), a flue gas outlet of the SCR denitration device (24) is connected with an induced draft fan (25) through a pipeline, and the induced draft fan (25) is communicated with a chimney (26) through a pipeline; the lower end of the residue incinerator (6) is communicated with a double-shaft cooler (3) through an expansion joint (4), a solid slag outlet of the double-shaft cooler (3) is communicated with a slag inlet of a water-cooled scraper slag remover (2), the lower end of a cyclone separator (13) is communicated with an inlet of the water-cooled scraper slag remover (2) through a star-shaped discharge valve (28), a replacement bin a (16) and a pipeline, and the lower end of a water-spraying cooling quench tower (15) is communicated with the inlet of the water-cooled scraper slag remover (2) through another star-shaped discharge valve (28), a replacement bin b (17) and a pipeline; a slag outlet of the water-cooled scraper slag remover (2) is communicated with a residue incineration warehouse; the top end of the waste heat boiler (11) is communicated with the steam drum (12); the residue atomizing spray gun (10) is communicated with the waste liquid buffer tank through a booster pump and a pipeline, the other interface of the residue atomizing spray gun (10) is connected with compressed air or a saturated steam pipeline with pressure, and residue liquid is atomized through the compressed air or saturated steam with pressure.

2. The incineration disposal system for the organic chemical refined distillation residue as recited in claim 1, wherein the inner wall of the residue incinerator (6) is coated with chrome corundum refractory castable (7) resistant to acid, alkali, corrosion and high temperature, a heat insulation castable (8) is arranged between the inner wall of the residue incinerator (6) and the chrome corundum refractory castable (7), and the residue incinerator is provided with a solid waste spreader (33).

3. The incineration disposal system for organic chemical industrial distillation residues as recited in claim 1, the waste heat boiler (11) adopts a vertical membrane water wall structure, a steam-water outlet pipe of a top header of the waste heat boiler (11) is communicated with a steam pocket (12), a plurality of groups of L-shaped membrane quenching screen type heating surfaces (29) and the steam pocket (12) are arranged in the waste heat boiler (11), an independently arranged centralized downcomer and an independently arranged steam-water riser form a closed circulation loop, four furnace walls of the waste heat boiler (11) are surrounded by the membrane water walls, an upper header and a lower header of the membrane water walls, the steam pocket (12), an independently arranged other downcomer and an independently arranged steam-water riser form another closed circulation loop, a plurality of diameter ash blowing openings are arranged on the side wall of the membrane water wall of the waste heat boiler (11) according to the arrangement position of a plurality of groups of L-shaped membrane wall quenching screen type heating surfaces (29) of the waste heat boiler (11).

4. The incineration disposal system for the residues generated in the chemical and organic chemical refining distillation of claim 1, wherein the upper half of the water spray cooling/quenching tower (15) is provided with a plurality of water spray quenching/atomizing spray guns.

5. The incineration disposal system for the residues in the organic chemical and chemical industrial fine distillation according to claim 1, wherein the bag filter (19) adopts on-line pulse soot blowing, the compressed air back-purged by the bag filter (19) is the compressed air heated by steam heat exchange, and an ash bucket with steam heat tracing is arranged at the lower end of the bag filter (19).

6. The incineration disposal system for the residues generated in the fine distillation of the organic chemical industry according to claim 1, wherein a multistage circulating spray washing pipe, a multistage cyclone separator, a multistage flue gas uniform distributor and a multistage packing layer are arranged in the deacidification tower (20), a demister consisting of baffle plates or wire meshes is installed at the top of the deacidification tower (20), and an outlet at the lower end of the deacidification tower (20) is communicated with a three-stage or multistage sedimentation tank for the deacidification liquid.

7. The organic chemical industry fine distillation residue incineration disposal system according to claim 1, wherein a combustor (22) is arranged on the flue gas reheater (23), the flue gas reheater (23) and the SCR denitration device (24) are in one tower, an ammonia injection port and a multi-stage staggered flue gas uniform pore plate are arranged between the flue gas reheater (23) and the SCR denitration device (24), the SCR denitration device (24) is composed of multi-stage denitration catalysts, and a manhole for overhauling or replacing the denitration catalysts is arranged between two adjacent stages of the denitration catalysts.

8. The incineration disposal system for the residues generated in the chemical and organic chemical refining distillation of claim 1, wherein the replacement bin a (16) and the replacement bin b (17) are respectively provided with a replacement nitrogen inlet (30), a safety valve (31) and a replacement nitrogen outlet (32), and the replacement nitrogen outlet (32) is connected to a flue gas inlet at the lower part of the deacidification tower (20) through a pipeline.

9. The incineration disposal system for the residues generated in the chemical and organic chemical industrial distillation of claim 1, wherein the venturi tube (18) is provided with a quicklime injection device interface and an activated carbon injection device interface.

10. The incineration disposal system for the residues generated in the chemical and organic chemical refining distillation of claim 1, wherein a demister (21) is installed in a pipeline communicating the deacidification tower (20) and the flue gas reheater (23).

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