CN109848191B - A device for continuous treatment of hazardous chemical waste with high salt and high COD - Google Patents
A device for continuous treatment of hazardous chemical waste with high salt and high COD Download PDFInfo
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- CN109848191B CN109848191B CN201910294262.6A CN201910294262A CN109848191B CN 109848191 B CN109848191 B CN 109848191B CN 201910294262 A CN201910294262 A CN 201910294262A CN 109848191 B CN109848191 B CN 109848191B
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/40—Valorisation of by-products of wastewater, sewage or sludge processing
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/20—Waste processing or separation
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Abstract
本发明公开了一种连续化处理高盐高COD化工危废的装置，包括预处理系统、水热解系统、催化重整系统、高浓盐水蒸发分盐系统、加热系统、辅助系统、甲烷综合利用系统和电源设备，预处理系统包括物料储存罐、计量装置、水箱、预处理混合装置、高压水泵、物料进料泵；水热解系统包括水热解反应器、气固分离器、混合进料泵；催化重整系统包括依次串联的一级反应器、二级反应器、三级反应器、四级反应器；高浓盐水蒸发分盐系统包括盐水箱、盐水泵、蒸发室、换热器；加热系统包括加热夹套一、加热夹套二，辅助系统包括惰性气体储存罐和惰性气体泵；甲烷综合利用系统包括依次与加热夹套一、加热夹套二以及四级反应器相串连的甲烷回收装置。
The invention discloses a device for continuous treatment of high-salt and high-COD chemical hazardous waste, including a pretreatment system, a hydropyrolysis system, a catalytic reforming system, a high-concentration brine evaporation and salt separation system, a heating system, an auxiliary system, and a methane synthesis system. Using the system and power supply equipment, the pretreatment system includes a material storage tank, a metering device, a water tank, a pretreatment mixing device, a high-pressure water pump, and a material feeding pump; the water pyrolysis system includes a water pyrolysis reactor, a gas-solid separator, a mixing feed Feed pump; catalytic reforming system includes first-stage reactor, second-stage reactor, third-stage reactor, and fourth-stage reactor in series; high-concentration brine evaporation and salt separation system includes brine tank, brine pump, evaporation chamber, heat exchange The heating system includes the first heating jacket, the second heating jacket, the auxiliary system includes the inert gas storage tank and the inert gas pump; the methane comprehensive utilization system includes the first heating jacket, the second heating jacket and the fourth-stage reactor in series connected methane recovery unit.
Description
Technical Field
The invention belongs to the technical field of chemical hazardous waste treatment, and particularly relates to a device for continuously treating high-salt high-COD chemical hazardous waste.
Background
The chemical hazardous waste refers to solid, semi-solid or slurry waste generated in the chemical production process, including unqualified products or intermediate products, by-products, waste catalysts, waste additives, unreacted raw materials, raw material impurities and the like generated in chemical reaction processes of decomposition, synthesis and the like in the chemical production process, and also includes waste directly discharged from a reaction device or discharged from a corresponding device when products are hung, separated and washed, dust discharged from an air pollution control facility, sludge generated in the wastewater treatment process, solid waste generated by equipment maintenance and accident leakage and the like.
The chemical hazardous waste has the following characteristics: (1) the production amount is large. The chemical hazardous waste accounts for more than 30% of the total amount of the whole industrial hazardous waste; (2) various types, high content of toxic substances and great harm to human health and environment. A considerable part of chemical hazardous wastes have the characteristics of acute toxicity, reactivity, corrosivity and the like, which can form great threats to human health and environment, and if the chemical hazardous wastes are not effectively treated, the chemical hazardous wastes can greatly affect human health and environment. (3) The potential of resource utilization is large. A considerable part of chemical hazardous waste is raw materials and byproducts of reaction, and valuable substances can be recycled through proper technical treatment. Therefore, chemical hazardous waste harmless treatment, recycling and energy regeneration are effectively realized, and the method plays an important role in improving pollution prevention and control level and industrial economic benefit.
Current plants for such waste disposal are primarily based on incineration and landfill technology. However, when incineration technology is used for treating such hazardous wastes, the following problems exist: (1) in a high-temperature molten state, the rotary kiln has serious scaling phenomenon and obvious reduction of thermal efficiency; (2) the corrosion phenomenon of the equipment is very serious; (3) most of the chlorine-containing salts generate a large amount of dioxin during incineration, thereby causing secondary pollution; (4) most of these hazardous wastes exist in a wet form, resulting in high energy consumption of incineration. When the safe landfill treatment of the hazardous wastes, the following problems exist: (1) a rigid landfill is needed, and the construction cost is high; (2) the occupied land area is large; (3) a large amount of high-COD and high-salt-content leachate can not be treated.
Disclosure of Invention
Aiming at the defects and shortcomings of the hazardous waste treatment device technology, the invention provides an economical, efficient and practical device for continuously treating high-salt and high-COD chemical hazardous waste.
The technical scheme of the invention is as follows: a device for continuously treating high-salt high-COD chemical hazardous waste comprises a pretreatment system, a aquathermolysis system, a catalytic reforming system, a high-concentration brine evaporation salt separation system, a heating system, an auxiliary system, a methane comprehensive utilization system and power supply equipment,
the pretreatment system comprises a material storage tank, a metering device, a water tank, a pretreatment mixing device, a high-pressure water pump and a material feeding pump, wherein the material storage tank is connected with the metering device, the metering device is connected to the pretreatment mixing device through the material pump, the water tank is connected to the pretreatment mixing device through the high-pressure water pump, and a stirrer is arranged in the pretreatment mixing device;
the hydrothermal decomposition system comprises a hydrothermal decomposition reactor, a gas-solid separator and a mixed feeding pump, the pretreatment mixing device is connected to the hydrothermal decomposition reactor through the mixed feeding pump, and the gas-solid separator is connected with the upper part of the hydrothermal decomposition reactor through a pyrolysis gas discharge pipe;
the catalytic reforming system comprises a primary reactor, a secondary reactor, a tertiary reactor and a quaternary reactor which are sequentially connected in series, wherein the upper end of the primary reactor is connected with a gas outlet of the gas-solid separator;
the high-concentration brine evaporation salt separation system comprises a brine tank, a brine pump, an evaporation chamber and a heat exchanger, wherein the brine tank is connected with the bottom of a hydrothermal reactor, the evaporation chamber is positioned above the brine tank, an inclined plate is arranged in the evaporation chamber, air holes and convex holes are formed in the inclined plate, a circulating pump is arranged in the evaporation chamber below the inclined plate, a small fan is arranged on the side wall of the evaporation chamber above the inclined plate, the heat exchanger is connected above the evaporation chamber through a pipeline, and the heat exchanger is connected with the brine tank through the brine pump;
the heating system comprises a first heating jacket and a second heating jacket, the first heating jacket is arranged outside the water tank, and the second heating jacket is arranged outside the pretreatment mixing device;
the auxiliary system comprises an inert gas storage tank and an inert gas pump, wherein the inert gas storage tank sends inert gas to the pretreatment mixing device and the hydrothermal decomposition reactor through the inert gas pump, and the inert gas storage tank is used for discharging oxygen in the pretreatment hydrolysis catalytic reforming process device;
the methane comprehensive utilization system comprises a methane recovery device which is sequentially connected with a heating jacket I, a heating jacket II and a four-stage reactor in series;
the power supply device supplies power to all the systems.
Furthermore, a first temperature detection device and a first pressure detection device are arranged in the pretreatment mixing device.
Furthermore, the hydrothermal reactor is internally provided with the tubes, materials are heated and decomposed in the tubes, and baffles are arranged among the tubes to ensure that no dead angle exists in the flowing process of a heat source among the tubes.
As another kind of scheme, the aquathermolysis reactor includes the retort, shell and tube heat transfer presss from both sides the cover, the aeration puddler, agitator motor, sealed bearing, shell and tube heat transfer presss from both sides the outside of cover setting at the retort, agitator motor sets up the top at the retort, sealed bearing sets up the bottom at the retort, the inside cavity of aeration puddler, transversely be equipped with 8 stirring horizontal poles on the aeration puddler, stirring horizontal pole's distal end is equipped with the exposure mouth, the upper end of aeration puddler is run through the retort top and is linked to each other with agitator motor, the lower extreme of aeration puddler runs through the retort bottom and links to each other with the sealed bearing upper end, the sealed bearing lower extreme passes through the inert gas pump and links to each other with the inert gas holding vessel, the sealed bearing lower extreme still links to. When the aeration stirring rod rotates, let in inert gas from aeration stirring rod bottom, and make it follow the aeration nozzle blowout, carry out the aeration stirring to the material, prevent that it from taking place to be heated the inequality, and inert gas's air current can carry out 360 degrees high pressure to the retort inner wall and erode, prevent that the material from taking place the adhesion at the retort wall, after finishing using, still can follow water tank through high pressure water pump two and take out water to aeration stirring rod bottom, make high pressure rivers spout from the aeration nozzle, can be used to wash the retort.
Furthermore, a second temperature detection device and a second pressure detection device are arranged in the hydrothermal reactor.
Furthermore, a third heating jacket is arranged outside the inert gas storage tank and is connected in series between the second heating jacket and the fourth-stage reactor. The inert gas in the inert gas storage tank is heated by the waste heat of methane, and is aerated and stirred in the aeration stirring rod, so that the heating efficiency of the materials in the reaction tank can be improved.
Furthermore, a pipeline between the gas-solid separator and the hydrothermal reactor is provided with a back pressure valve and an adjusting valve.
Furthermore, the first-stage reactor, the second-stage reactor, the third-stage reactor and the fourth-stage reactor are tubular reactors, a circular reaction cavity is formed in the middle of each tubular reactor, a rotating shaft transversely penetrates through the circular reaction cavity, a driving motor is connected to the outer portion of the rotating shaft, 6 blade boxes are arranged on the rotating shaft, and catalysts are contained in the blade boxes. The gas goes from top to bottom, and the rotating shaft rotates anticlockwise to be in contact with the gas, so that the contact area of the gas and the catalyst can be increased, and the gas can be prevented from flowing unsmoothly.
Furthermore, catalysts in the blade boxes corresponding to the first-stage reactor, the second-stage reactor, the third-stage reactor and the fourth-stage reactor are respectively an activated carbon AlNiCo magnetic catalyst, an attapulgite nickel-based catalyst, a ferrochrome fiber catalyst and a nano nickel-based catalyst.
Compared with the prior art, the invention has the beneficial effects that:
(1) the invention utilizes a hydrothermal decomposition technology to react and decompose organic matters and water under the conditions of high temperature and high pressure to convert the organic matters into energy substances such as liquid fuel or gas fuel and the like. Compared with the existing method mainly adopting incineration and landfill, the reaction takes water as a raw material, wet materials do not need to be dried, energy is saved, the reaction is thorough under the conditions of high temperature and high pressure, the problems of secondary pollution and the like caused by organic matter residue can be avoided, and the quality of products obtained by subsequent salt recovery can be improved.
(2) In the catalytic reforming process, under the action of the special catalyst of each stage reactor, the impurities which are useless in the pyrolysis gas and influence the methanation catalyst can be effectively removed, and various low-carbon compounds and water are reformed to synthesize the methane gas with higher utilization value. The produced methane gas can be used as an energy source for system operation, and the surplus methane gas can be sold in the form of electricity, steam or natural gas.
(3) The low-temperature evaporation adopted by the invention is characterized in that a special equipment structure is adopted, a fast flowing liquid film can cause very low negative pressure in an air hole on the inclined plate surface in an evaporation chamber, and a huge airflow can be pushed up to pass through the water film by only one small fan, so that a great exchange surface is generated between gas and liquid. When liquid flows downwards along the inclined plate, slight negative pressure is generated in the downward direction due to cavitation erosion, and a plurality of protruding holes are formed in the surface of the inclined plate, so that gas below the plate passes through plate holes to enter flowing liquid, the liquid is stretched into bubbles, and the gas and the liquid are contacted for a time period which is enough to change the gas into saturated steam.
In a word, the method can efficiently treat the high-salt high-COD hazardous waste without generating secondary pollution, and the generated salt does not contain organic matters; the water required by the reaction can be recycled and is not discharged; the organic matters can be changed into clean energy after being decomposed, and the chemical hazardous waste recycling is fully realized.
Drawings
FIG. 1 is a schematic view of an overall apparatus of example 1 of the present invention;
FIG. 2 is a schematic view of the whole apparatus of example 2 of the present invention;
FIG. 3 is a schematic view of the structure of a hydrothermal reactor in example 2 of the present invention;
fig. 4 is a schematic structural view of a swash plate in embodiments 1 and 2 of the present invention;
FIG. 5 is a schematic view of a partial structure of a hydrothermolysis reactor in example 1 of the present invention;
FIG. 6 is a schematic view showing the external structure of a tubular reactor in examples 1 and 2 of the present invention;
FIG. 7 is a schematic view showing the internal structure of a tubular reactor in examples 1 and 2 of the present invention;
wherein, 1-a material storage tank, 2-a metering device, 3-a water tank, 4-a pretreatment mixing device, 5-a high-pressure water pump, 6-a material feeding pump, 7-a stirrer, 8-a hydrothermal decomposition reactor, 9-a gas-solid separator, 10-a mixed feeding pump, 11-a first-stage reactor, 12-a second-stage reactor, 13-a third-stage reactor, 14-a fourth-stage reactor, 15-a brine tank, 16-a brine pump, 17-an evaporation chamber, 18-a heat exchanger, 19-an inclined plate, 20-an air hole, 21-a circulating pump, 22-a first heating jacket, 23-a second heating jacket, 24-an inert gas storage tank, 25-an inert gas pump, 26-a first temperature detection device, 27-a first pressure detection device, a second pressure detection device, a, 28-tubes, 29-baffle, 30-reaction tank, 31-tube type heat exchange jacket, 32-aeration stirring rod, 33-stirring motor, 34-sealing bearing, 35-high pressure water pump II, 36-temperature detection device II, 37-pressure detection device II, 38-heating jacket III, 39-back pressure valve, 40-regulating valve, 41-circular reaction cavity, 42-rotating shaft, 43-driving motor, 44-blade box, 45-convex hole, 46-small fan, 47-methane recovery device, 48-stirring cross bar and 49-aeration nozzle.
Detailed Description
The following description of the embodiments of the present invention will be made with reference to the accompanying drawings 1-7, but the invention is not limited thereto.
Example 1
As shown in FIG. 1, a device for continuously treating high-salt high-COD chemical hazardous waste comprises a pretreatment system, a hydrothermolysis system, a catalytic reforming system, a high-concentration brine evaporation salt separation system, a heating system, an auxiliary system, a methane comprehensive utilization system and power supply equipment,
the pretreatment system comprises a material storage tank 1, a metering device 2, a water tank 3, a pretreatment mixing device 4, a high-pressure water pump 5 and a material feeding pump 6, wherein the material storage tank 1 is connected with the metering device 2, the metering device 2 is connected to the pretreatment mixing device 4 through the material pump 6, the water tank 3 is connected to the pretreatment mixing device 4 through the high-pressure water pump 5, and a stirrer 7 is arranged in the pretreatment mixing device 4;
the water pyrolysis system comprises a water pyrolysis reactor 8, a gas-solid separator 9 and a mixed feeding pump 10, the pretreatment mixing device 4 is connected to the water pyrolysis reactor 8 through the mixed feeding pump 10, and the gas-solid separator 9 is connected above the water pyrolysis reactor 8; as shown in FIG. 5, the hydrothermal reactor 8 is provided with the tubes 28, the material is decomposed by heating in the tubes 28, and the baffles 29 are arranged between the tubes 28 to ensure that no dead angle exists in the flowing process of the heat source between the tubes 28. The pretreatment mixing device 4 is internally provided with a first temperature detection device 26 and a first pressure detection device 27. And a second temperature detection device 36 and a second pressure detection device 37 are also arranged in the hydrothermal reactor 8. A back pressure valve 39 and an adjusting valve 40 are arranged on a pipeline between the gas-solid separator 9 and the water pyrolysis reactor 8.
The catalytic reforming system comprises a primary reactor 11, a secondary reactor 12, a tertiary reactor 13 and a quaternary reactor 14 which are sequentially connected in series, wherein the upper end of the primary reactor 11 is connected with a gas outlet of the gas-solid separator 9; as shown in fig. 6-7, the first-stage reactor 11, the second-stage reactor 12, the third-stage reactor 13, and the fourth-stage reactor 14 are all tubular reactors, a circular reaction chamber 41 is disposed in the middle of the tubular reactor, a rotating shaft 42 transversely penetrates through the circular reaction chamber 41, a driving motor 43 is connected to the outside of the rotating shaft 42, 6 blade boxes 44 are disposed on the rotating shaft 42, and a catalyst is filled in the blade boxes 44. The gas goes from top to bottom, and the rotating shaft 42 rotates counterclockwise to contact with the gas, so that the contact area between the gas and the catalyst can be increased, and the gas flow is prevented from being unsmooth. Wherein, the catalysts in the blade boxes 44 corresponding to the first-stage reactor 11, the second-stage reactor 12, the third-stage reactor 13 and the fourth-stage reactor 14 are respectively an activated carbon alnico magnetic catalyst, an attapulgite nickel-based catalyst, a ferrochrome fiber catalyst and a nanometer nickel-based catalyst.
The high-concentration brine evaporation salt separation system comprises a brine tank 15, a brine pump 16, an evaporation chamber 17 and a heat exchanger 18, wherein the brine tank 15 is connected with the bottom of a hydrothermal reactor 8, the evaporation chamber 17 is positioned above the brine tank 15, an inclined plate 19 is arranged in the evaporation chamber 17, as shown in fig. 4, an air hole 20 and a convex hole 45 are distributed on the inclined plate 19, a circulating pump 21 is arranged in the evaporation chamber 17 below the inclined plate 19, a small fan 46 is arranged on the side wall of the evaporation chamber 17 above the inclined plate 19, the heat exchanger 18 is connected above the evaporation chamber 17 through a pipeline, and the heat exchanger 18 is connected with the brine tank 15 through the brine pump;
the heating system comprises a first heating jacket 22 and a second heating jacket 23, the first heating jacket 22 is arranged outside the water tank 3, and the second heating jacket 23 is arranged outside the pretreatment mixing device 4;
the auxiliary system comprises an inert gas storage tank 24 and an inert gas pump 25, wherein the inert gas storage tank 24 sends inert gas to the pretreatment mixing device 4 and the hydrothermal reactor 8 through the inert gas pump 25, and is used for removing oxygen in the pretreatment hydrolysis catalytic reforming process device;
the methane comprehensive utilization system comprises a methane recovery device 47 which is sequentially connected with a first heating jacket 22, a second heating jacket 23 and a four-stage reactor 14 in series;
the power supply device supplies power to all the systems.
The working method of the embodiment comprises the following steps:
pretreatment: incoming materials firstly enter a material storage tank 1, are metered by a metering device 2 and then are sent to a pretreatment mixing device 4 through a pipeline by a material feeding pump 6, water in a water tank 3 is sent to the pretreatment mixing device 4 through a high-pressure water pump 5, a stirrer 7 is started, and the water and the materials are uniformly mixed and then enter a tube array 28 of a hydrothermal decomposition reactor 8 through a mixing feeding pump 10;
hydrothermal decomposition: controlling the internal temperature to be 300 ℃, the pressure to be 20MPa and the reaction time to be 105min, decomposing and gasifying more than 99 percent of organic matters, opening the regulating valve 40, separating the formed high-temperature pyrolysis gas through the gas-solid separator 9, and separating solid substances carried by the pyrolysis gas;
catalytic reforming: high-temperature pyrolysis gas is sent to the top of a first-stage reactor 11, substances with toxic effects on catalytic reforming are removed under the catalytic action of an activated carbon alnico magnetic catalyst, the pyrolysis gas enters a second-stage reactor 12 from the bottom, multi-carbon compounds such as C2 and C3 which may exist are decomposed under the action of an attapulgite nickel-based catalyst to form monocarbon compounds, the monocarbon compounds are then sent to a third-stage reactor 13, the carbon-containing compounds in the mixed gas react with water under the action of a ferrochrome fiber catalyst, hydrogen in the water is recovered, the reacted mixed gas enters a fourth-stage reactor 14, and most of carbon and hydrogen in the mixed gas are synthesized into methane under the action of a nanometer nickel-based catalyst. Finally, high-temperature methane gas sequentially passes through the second heating jacket 23 and the first heating jacket 22, part of heat in the high-temperature methane gas is recovered, the temperature in the pretreatment mixing device 4 and the temperature in the water tank 3 are increased, meanwhile, the temperature of the methane gas is reduced, and finally the methane gas is sent to a methane recovery device 47;
low-temperature evaporation: after high COD chemical industry hazardous waste decomposes the organic matter through hydrothermal reaction ware 8, remaining salt gets into brine tank 15 with the solution form, send salt solution to heat exchanger 18 by brine pump 16 and heat to required temperature after, hot salt solution passes through the pipeline and gets into in the evaporating chamber 17, and through circulating pump 21 with salt solution equipartition on swash plate 19, salt solution flows along swash plate 19 face, when the lug hole 45 that distributes on the swash plate 19, the wind that small-size fan 46 introduced is through contacting with gas pocket 20, and form little negative pressure here, the negative pressure stretches into the bubble with liquid, the time of gas-liquid contact is enough to make gas become saturated steam and discharge, retrieve and contain the salt crystallization.
The TVOC value of the methane generated in the example was measured to be 0.05ppm, and the content of organic matter in the salt-containing crystals obtained in the example was measured to be 0.00% by the burning method.
Example 2
This embodiment is substantially the same as embodiment 1 except that:
(1) as shown in fig. 3, the hydrothermal reactor 8 includes a reaction tank 30, a tubular heat exchange jacket 31, an aeration stirring rod 32, a stirring motor 33, and a sealing bearing 34, wherein the tubular heat exchange jacket 31 is disposed outside the reaction tank 30, the stirring motor 33 is disposed at the top of the reaction tank 30, the sealing bearing 34 is disposed at the bottom of the reaction tank 30, the aeration stirring rod 32 is hollow, 8 stirring cross rods 48 are transversely disposed on the aeration stirring rod 32, an aeration nozzle 49 is disposed at the distal end of each stirring cross rod 48, the upper end of the aeration stirring rod 32 penetrates through the top of the reaction tank 30 and is connected with the stirring motor 33, the lower end of the aeration stirring rod 32 penetrates through the bottom of the reaction tank 30 and is connected with the upper end of the sealing bearing 34, the lower end of the sealing bearing 34 is connected with an inert gas storage tank 24 through an inert gas pump 25, and the lower end of the sealing bearing 34 is further. When aeration puddler 32 rotated, let in inert gas from aeration puddler 32 bottom, and make it spout from aeration mouth 49, carry out the aeration stirring to the material, prevent that it from taking place to be heated unevenly, and inert gas's air current can carry out 360 degrees high pressure to wash away to retort 30 inner wall, prevent that the material from taking place the adhesion at retort 30 wall, after finishing using, still can draw water to aeration puddler 32 bottom from water tank 3 through two 35 high pressure water pumps, make high-pressure rivers spout from aeration mouth 49, can be used to wash retort 30.
(2) As shown in FIG. 2, the inert gas storage tank 24 is externally provided with a heating jacket three 38, and the heating jacket three 38 is connected in series between the heating jacket two 23 and the four-stage reactor 14. The inert gas in the inert gas storage tank 24 is heated by the residual heat of the methane, and is aerated and stirred in the aeration stirring rod 32, so that the heating efficiency of the materials in the reaction tank 30 can be improved.
The working method of the embodiment comprises the following steps:
pretreatment: the incoming material firstly enters a material storage tank 1, is metered by a metering device 2 and then is sent to a pretreatment mixing device 4 by a material feeding pump 6 through a pipeline, water in a water tank 3 is sent to the pretreatment mixing device 4 by a high-pressure water pump 5, a stirrer 7 is started, and after the water and the material are uniformly mixed, the mixture enters a reaction tank 30 of a hydrothermal decomposition reactor 8 through a mixed feeding pump 10;
hydrothermal decomposition: introducing inert gas from the bottom of the aeration stirring rod 32, spraying the inert gas from the aeration nozzle 49, carrying out aeration stirring on the materials, preventing the materials from being unevenly heated, washing the inner wall of the reaction tank 30 at 360 ℃ under high pressure by the airflow of the inert gas, preventing the materials from being adhered to the wall of the reaction tank 30, controlling the internal temperature to be 400 ℃, the pressure to be 20MPa, the reaction time to be 105min, decomposing and gasifying more than 99% of organic matters, opening the regulating valve 40, separating the formed high-temperature pyrolysis gas through the gas-solid separator 9, and separating solid substances carried by the pyrolysis gas;
catalytic reforming: high-temperature pyrolysis gas is sent to the top of a first-stage reactor 11, substances with toxic effects on catalytic reforming are removed under the catalytic action of an activated carbon alnico magnetic catalyst, the pyrolysis gas enters a second-stage reactor 12 from the bottom, multi-carbon compounds such as C2 and C3 which may exist are decomposed under the action of an attapulgite nickel-based catalyst to form monocarbon compounds, the monocarbon compounds are then sent to a third-stage reactor 13, the carbon-containing compounds in the mixed gas react with water under the action of a ferrochrome fiber catalyst, hydrogen in the water is recovered, the reacted mixed gas enters a fourth-stage reactor 14, and most of carbon and hydrogen in the mixed gas are synthesized into methane under the action of a nanometer nickel-based catalyst. Finally, high-temperature methane gas sequentially passes through the third heating jacket 38, the second heating jacket 23 and the first heating jacket 22, part of heat in the high-temperature methane gas is recovered, the temperature in the inert gas storage tank 24, the pretreatment mixing device 4 and the water tank 3 is increased, the temperature of the methane gas is reduced at the same time, and finally the methane gas is sent to a methane recovery device 47; the inert gas in the inert gas storage tank 24 is heated by the residual heat of the methane, and is aerated and stirred in the aeration stirring rod 32, so that the heating efficiency of the materials in the reaction tank 30 can be improved.
Low-temperature evaporation: after high COD chemical industry hazardous waste decomposes the organic matter through hydrothermal reaction ware 8, remaining salt gets into brine tank 15 with the solution form, send salt solution to heat exchanger 18 by brine pump 16 and heat to required temperature after, hot salt solution passes through the pipeline and gets into in the evaporating chamber 17, and through circulating pump 21 with salt solution equipartition on swash plate 19, salt solution flows along swash plate 19 face, when the lug hole 45 that distributes on the swash plate 19, the wind that small-size fan 46 introduced is through contacting with gas pocket 20, and form little negative pressure here, the negative pressure stretches into the bubble with liquid, the time of gas-liquid contact is enough to make gas become saturated steam and discharge, retrieve and contain the salt crystallization.
The TVOC value of the methane generated in the example was measured to be 0.03ppm, and the content of organic matter in the salt-containing crystals obtained in the example was measured to be 0.00% by the burning method.
Finally, it should be noted that: the above examples are only intended to illustrate the technical solution of the present invention, but not to limit it; although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; and such modifications or substitutions do not depart from the spirit and scope of the corresponding technical solutions of the embodiments of the present invention.
Claims (9)
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Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1188776A (en) * | 1997-01-20 | 1998-07-29 | 株式会社神户制钢所 | Waste decomposition method and device |
| CN1320267A (en) * | 1998-07-28 | 2001-10-31 | 斯塔德斯维克公司 | Pyrolytic decomposition of organic wastes |
| TW200420532A (en) * | 2002-08-12 | 2004-10-16 | Basf Ag | Preparation of acid formates and their use |
| CN101189190A (en) * | 2005-04-27 | 2008-05-28 | 环境能量技术股份有限公司 | Organic waste treatment equipment and treatment methods |
| CN102015583A (en) * | 2008-02-26 | 2011-04-13 | Ab-Cwt有限责任公司 | Methods and apparatus for converting waste materials into fuels and other useful products |
| CN106277676A (en) * | 2016-08-31 | 2017-01-04 | 王焕升 | A kind of for disposing the chemical industry danger device of waste sludge and technique |
| CN206417959U (en) * | 2016-11-29 | 2017-08-18 | 碳氢技术工程管理（武汉）有限公司 | A kind of device of combined treatment high salt and high COD sewage |
| CN107673406A (en) * | 2017-11-14 | 2018-02-09 | 黄林海 | The production system and its production method of a kind of rutile titanium dioxide |
| CN208038219U (en) * | 2018-01-08 | 2018-11-02 | 山东特保罗环保节能科技有限公司 | A kind of high-salt wastewater processing equipment |
| CN108793551A (en) * | 2018-06-07 | 2018-11-13 | 山东理工大学 | A kind of processing method and its processing unit of high COD organic wastewater with high salt |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8177946B2 (en) * | 2007-08-09 | 2012-05-15 | Lawrence Livermore National Security, Llc | Electrochemical formation of hydroxide for enhancing carbon dioxide and acid gas uptake by a solution |
-
2019
- 2019-04-12 CN CN201910294262.6A patent/CN109848191B/en active Active
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1188776A (en) * | 1997-01-20 | 1998-07-29 | 株式会社神户制钢所 | Waste decomposition method and device |
| CN1320267A (en) * | 1998-07-28 | 2001-10-31 | 斯塔德斯维克公司 | Pyrolytic decomposition of organic wastes |
| TW200420532A (en) * | 2002-08-12 | 2004-10-16 | Basf Ag | Preparation of acid formates and their use |
| CN101189190A (en) * | 2005-04-27 | 2008-05-28 | 环境能量技术股份有限公司 | Organic waste treatment equipment and treatment methods |
| CN102015583A (en) * | 2008-02-26 | 2011-04-13 | Ab-Cwt有限责任公司 | Methods and apparatus for converting waste materials into fuels and other useful products |
| CN106277676A (en) * | 2016-08-31 | 2017-01-04 | 王焕升 | A kind of for disposing the chemical industry danger device of waste sludge and technique |
| CN206417959U (en) * | 2016-11-29 | 2017-08-18 | 碳氢技术工程管理（武汉）有限公司 | A kind of device of combined treatment high salt and high COD sewage |
| CN107673406A (en) * | 2017-11-14 | 2018-02-09 | 黄林海 | The production system and its production method of a kind of rutile titanium dioxide |
| CN208038219U (en) * | 2018-01-08 | 2018-11-02 | 山东特保罗环保节能科技有限公司 | A kind of high-salt wastewater processing equipment |
| CN108793551A (en) * | 2018-06-07 | 2018-11-13 | 山东理工大学 | A kind of processing method and its processing unit of high COD organic wastewater with high salt |
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