A zero-emission resource utilization system for high-salt and chlorine-containing organic waste liquid

Abstract

The invention discloses a zero-emission resource utilization system for high-salt and chlorine-containing organic waste liquid, which relates to the technical field of industrial waste treatment, and comprises a high-temperature incineration module, a rapid cooling module for curbing dioxin generation, a gas-solid separation module, an HCl separation module, an alkali washing and neutralization module, a low-temperature denitration module, a water treatment module and a molten salt cooling, conveying and packaging module, wherein the high-temperature incineration module, the rapid cooling module for curbing dioxin generation, the gas-solid separation module, the HCl separation module, the alkali washing and neutralization module and the low-temperature denitration module are sequentially connected through a flue. The invention has a reasonable design and a compact structure, and utilizes the high-temperature incineration principle to melt the inorganic salt generated by the incineration of the waste liquid into molten salt, cool it and then package it, and recover the high-purity inorganic salt. Utilizing the principle that HCl gas is easily soluble in water, a water spray mist is used in a secondary absorption tower to absorb the HCl gas in the flue gas, and dilute hydrochloric acid is recovered. A waste heat boiler is used to recover the heat energy in the flue gas, and the by-product steam is provided for users. The invention transforms waste into treasure, not only meets the national environmental protection and energy-saving requirements, but also realizes the resource utilization of waste, meets the national strategic requirements for sustainable development, provides a scientific method for enterprises to reduce burdens and increase efficiency, and is suitable for promotion and use.

Description

Technical Field

[0001] The invention relates to the technical field of industrial waste treatment, in particular to a zero-emission resource utilization system for high-salt and chlorine-containing organic waste liquid. Background Art

[0002] Today's chemical industry is becoming more and more developed, and the amount of waste liquid and waste gas generated is increasing. The country's requirements for environmental protection are also getting higher and higher. With the development of production, chemical production equipment is being built rapidly on a large scale, the output of hazardous waste is increasing, and the requirements for hazardous waste treatment technology are also getting higher and higher. Incineration technology has the advantages of thorough treatment, high efficiency, low investment, and small land occupation. It has become an important technology in the chemical industry. Incineration equipment has also become an important part of chemical equipment. Incineration of organic waste is an effective means of treating organic matter in waste liquid by deep oxidation of air under high temperature conditions. Usually, organic compound waste is incinerated at high temperature and converted into CO 2 and H 2 O and then discharged into the atmosphere. As long as the temperature in the incinerator is greater than 800℃ and the waste has a long enough residence time in the high temperature zone of the furnace, the waste can basically be completely decomposed and pollution-free emissions can be achieved. However, for some chlorine-containing organic waste liquids and waste gases generated in chemical production, HCl and free chlorine will be emitted during high-temperature incineration. Chlorine is highly corrosive and will not only cause high-temperature corrosion damage to the heating surface, but also cause low-temperature corrosion of the tail heating surface and flue; more seriously, chlorine is an extremely toxic medium and can easily cause huge pollution to the environment. All countries have strict regulations on this. Therefore, how to achieve the standard discharge of chlorine-containing waste is an important issue facing engineering designers.

[0003] For example, the patent with the authorization number CN 101634453 B can solve the problem of chlorine-containing waste very well, but it still has some shortcomings. It will produce a large amount of dilute hydrochloric acid. After neutralization by alkali washing, it consumes a large amount of sodium hydroxide solution, and still produces a large amount of high-salt wastewater, which needs to be discharged into the sewage treatment system for standard treatment. The sacrificial alkali solution is used to remove HCL, and the operating cost is high. The patent with the patent number CN201520057318 proposes "a treatment device for chlorine-containing and salt-containing organic waste liquid". The process flow adopted by the invention is: incineration boiler-radiation cooling chamber-quencher-Venturi dust collector-gas-liquid separator-induced draft fan-chimney. The advantage of this device is that it adopts an incineration treatment method, the furnace temperature exceeds 1200℃, the organic matter removal rate is high, and the salt can be collected in liquid form and the sewage can be recycled. The disadvantage is that the HCl gas and NOX generated by incineration have not undergone special environmental protection treatment, so the flue gas generated after incineration is difficult to achieve standard emission in accordance with the control requirements of pollutant emissions stipulated in national environmental protection standards. Saving costs and achieving zero emissions in recycling are the ultimate goals of industrial waste treatment, and are what environmental protection equipment workers need to continue to work hard on. In response to the above problems, our company has proposed a zero-emission resource utilization system for high-salt and chlorine-containing organic waste liquid. Summary of the invention

[0004] The purpose of the present invention is to provide a zero-discharge resource utilization system for high-salt and chlorine-containing organic waste liquid to solve the problems raised in the above background technology.

[0005] To achieve the above-mentioned purpose, the present invention provides the following technical solutions: a zero-emission resource utilization system for high-salt and chlorine-containing organic waste liquid, comprising a high-temperature incineration module, a rapid cooling module for curbing dioxin generation, a gas-solid separation module, an HCl separation module, an alkali washing and neutralization module, a low-temperature denitrification module, a water treatment module and a molten salt cooling, conveying and packaging module, wherein the high-temperature incineration module, the rapid cooling module for curbing dioxin generation, the gas-solid separation module, the HCl separation module, the alkali washing and neutralization module and the low-temperature denitrification module are sequentially connected through a flue, the high-temperature incineration module comprises an adiabatic incinerator, two layers of main burners are arranged in the middle of the adiabatic incinerator, an atomizing spray gun is installed at the upper end of the adiabatic incinerator, and the adiabatic A waste liquid pipeline and a compressed air pipeline are connected to the upper outer side of the incinerator, a waste liquid booster pump and a waste liquid buffer tank are connected to the front end of the waste liquid pipeline, a natural gas pipeline and an air pipeline are connected to the left side of the adiabatic boiler, a combustion-supporting blower is connected to the air pipeline, the bottom of the adiabatic incinerator is connected to a waste heat boiler, a supplementary combustion burner is installed inside the waste heat boiler, a soot blowing device is provided on the right side of the waste heat boiler, a steam drum is provided on the upper side of the adiabatic boiler, the lower end of the steam drum is connected to the internal heating surface of the waste heat boiler through a pipeline, a saturated steam pipeline is connected to the upper end of the steam drum, a desalted and deoxygenated water pipeline is connected to the right end of the steam drum, and a boiler feed water pump is connected to the desalted and deoxygenated water pipeline;

[0006] The quenching module for curbing dioxin generation includes a quenching tower, a quenching spray gun, a quenching water pump, and a quenching water tank. A quenching spray gun is installed on the upper part of the quenching tower. The upper right end of the quenching tower is connected to the quenching water tank through a pipeline and a quenching water pump. The right end of the quenching water tank is connected to a desalting and deoxygenating water pipeline. The lower end of the quenching tower is connected to a quenching tower replacement bin through a pipeline. The right end of the quenching tower is connected to a gas-solid separation module through a flue.

[0007] The gas-solid separation module includes a bag-type dust collector or a ceramic membrane gas-solid separator and a compressed air buffer tank. The upper left end of the bag-type dust collector or the ceramic membrane gas-solid separator is connected to the compressed air buffer tank through a pipeline, the right end of the compressed air buffer tank is connected to the compressed air pipeline, the lower end of the bag-type dust collector or the ceramic membrane gas-solid separator is connected to the bag-type replacement bin through a pipeline, the upper right end of the quenching tower replacement bin is connected in parallel to the flue between the quenching tower and the bag-type dust collector or the ceramic membrane gas-solid separator through the flue, the upper right end of the bag-type replacement bin is connected in parallel to the main flue at the outlet of the bag-type dust collector or the ceramic membrane gas-solid separator through the flue, and the lower left ends of the quenching tower replacement bin and the bag-type replacement bin are both connected to a nitrogen pipeline;

[0008] The HCl separation module includes a pre-cooling tower, a primary absorption tower, a circulating acid tank, a heat exchanger, an acid storage tank, a secondary absorption tower, and a secondary heat exchanger. A cooling spray gun is installed at the upper end of the pre-cooling tower. The upper end of the pre-cooling tower is connected to the primary heat exchanger through a pipeline. The upper end of the heat exchanger is connected to the circulating acid tank through a pipeline and a primary circulation pump. The upper right end of the circulating acid tank is connected to the acid storage tank through a pipeline. The right end of the acid storage tank is connected to a hydrochloric acid pipeline and a hydrochloric acid delivery pump. The bottom right side of the pre-cooling tower is connected to the storage tank at the bottom of the primary absorption tower through a pipeline. The upper left end of the primary absorption tower is connected between the pre-cooling tower and the heat exchanger through a pipeline. The lower right end of the primary absorption tower is connected to the acid storage tank and the circulating acid tank through a pipeline and a primary extraction pump, respectively. The right side of the primary absorption tower is connected to the secondary absorption tower through a flue. A secondary heat exchanger is provided on the left side of the secondary absorption tower. The lower end of the secondary heat exchanger is connected to the storage tank at the bottom of the secondary absorption tower through a pipeline and a secondary circulation pump. The pipeline above the secondary circulation pump is also connected to the bottom of the primary absorption tower. The upper end of the secondary heat exchanger is connected to the middle and upper end of the secondary absorption tower through a pipeline. The upper right end of the secondary absorption tower is connected to a high-position water storage tank through a pipeline, and the upper left end of the high-position water storage tank is connected to a desalted and deoxygenated water pipeline;

[0009] The alkali washing and neutralization module comprises an alkali washing tower, the upper left end of which is connected to an alkali washing tank through a pipeline and an alkali washing circulation pump, the right end of which is connected to an alkali solution pipeline, the upper right end of which is connected to a high-level water storage tank and a waste liquid buffer tank through pipelines, respectively, and the upper left end of which is connected to a storage tank in the alkali washing tower through a pipeline and an alkali washing extraction pump;

[0010] The low-temperature denitration module includes a denitration device, a denitration solution preparation tank, a denitration solution buffer tank, a static mixer, and a denitration solution atomizing nozzle. A flue gas heater is installed at the upper end of the denitration device, and a flue gas heater burner is arranged inside the flue gas heater. The left end of the flue gas heater burner is connected to a natural gas pipeline and an air pipeline. A static mixer is arranged on the right side of the denitration device. A desalination and deoxygenation water pipeline is connected to the right end of the static mixer. The upper end of the static mixer is connected to the denitration solution buffer tank through a pipeline and a denitration solution booster pump. The desalination and deoxygenation water pipeline is connected to the upper right end of the denitration solution buffer tank. The upper left end of the denitration solution buffer tank is connected to the denitration solution preparation tank through a pipeline and a denitration delivery pump. The right end of the denitration solution preparation tank is connected to the desalination and deoxygenation water pipeline and the denitration feeding pipeline. The lower left end of the denitration device is connected to the bottom of the chimney through a flue and an induced draft fan.

[0011] The water treatment module includes a deaerator, the left and right sides of the lower end of the deaerator are connected to desalinated and deoxygenated water pipelines, and the upper end of the deaerator is connected to a low-pressure steam pipeline;

[0012] The molten salt cooling, conveying and packaging module includes a double-axis cooler, a water-cooled scraper slag remover and a packaging device. The middle upper end of the water-cooled scraper slag remover is connected to the double-axis cooler through a pipeline, the upper end of the double-axis cooler is connected to the bottom of the waste heat boiler through a pipeline, the left end of the double-axis cooler is connected to a circulating cooling water supply pipeline and a circulating cooling water return pipeline, the lower end of the water-cooled scraper slag remover is connected to a circulating cooling water supply pipeline and a circulating cooling water return pipeline, the upper right end of the water-cooled scraper slag remover is respectively connected to the bottom of the quenching tower replacement bin and the bag replacement bin through pipelines, and the leftmost side of the water-cooled scraper slag remover is provided with a packaging device;

[0013] Further: the combustion temperature of the adiabatic incineration boiler is 1200°C, the waste heat boiler adopts a membrane wall type, and is composed of a salt collection chamber, a quenching chamber and a molten salt pool. The salt collection chamber is arranged at the lower part of the adiabatic incinerator, and a refractory furnace wall is laid inside the membrane wall of the salt collection chamber. The quenching chamber is composed of a membrane water-cooled wall plus a water-cooled screen, and a steam soot blower is arranged in the quenching chamber.

[0014] Furthermore: the first-level absorption tower is made of fiberglass, and is provided with three layers of absorption filler layers inside the first-level absorption tower. A first-level absorption nozzle is provided on the upper end of each absorption filler layer. Ball ring fillers are arranged in the second-level absorption tower, and a second-level absorption nozzle is provided on the upper end of the ball ring filler. A bubble layer is provided on the upper end of the second-level absorption nozzle.

[0015] Furthermore: the first-stage heat exchanger and the second-stage heat exchanger are both graphite heat exchangers, and the left ends of the first-stage heat exchanger and the second-stage heat exchanger are connected to a circulating cooling water supply pipe and a circulating cooling water return pipe.

[0016] Furthermore: an alkali washing packing layer is provided at the upper end of the alkali washing tower, and an alkali washing spray nozzle is provided at the upper end of the alkali washing packing layer.

[0017] Further: the denitrification device adopts a low-temperature denitrification method, a three-layer denitrification filler layer is arranged in the middle of the denitrification device, a denitrification solution atomizing nozzle is arranged above the denitrification filler layer, the left outer end of the denitrification solution atomizing nozzle is connected to a static mixer through a pipeline, an agitator is arranged in the denitrification solution preparation tank, and the denitrification agent adopts urea solution as a denitrification catalyst, and the temperature is controlled at 180~260℃.

[0018] Furthermore: the flue gas temperature in the quenching tower drops rapidly from 550°C to 180°C within 1 second.

[0019] Compared with the prior art, the present invention has the following beneficial effects:

[0020] 1. The waste heat boiler is directly arranged at the bottom of the incinerator, and the molten salt produced by incineration falls directly into the molten salt pool in the waste heat boiler salt collection chamber, ensuring that the temperature of the molten salt is always maintained above the melting point of the salt at 100°C, thus avoiding the problem of salt solidification and adhesion to the wall;

[0021] 2. The heating surface of the waste heat boiler salt collection chamber is covered with refractory castables to avoid the problem of molten salt directly contacting the membrane wall and causing corrosion to the membrane wall;

[0022] 3. The secondary absorption tower adopts a bubble layer, which uses clean water to absorb the HCl gas carried in the flue gas. It is used in conjunction with the filler layer to achieve higher absorption efficiency.

[0023] 4. Chlorine-containing and salt-containing organic waste liquid can be processed and recycled to recover dilute hydrochloric acid and by-product salt, which is in line with the national sustainable development strategy;

[0024] 5. While treating the organic waste liquid to meet environmental standards, the organic chemical energy in the waste liquid can be effectively utilized. After incineration and conversion into heat energy, saturated steam is produced as a by-product for users to use;

[0025] 6. This system can achieve zero wastewater discharge. The brine produced by the alkali washing tower can be sent back to the incinerator for incineration. The solid salt produced after incineration is collected, and part of the water carried in the flue gas is collected by the alkali washing tower and the two-stage absorption tower for recycling;

[0026] The invention has reasonable design and compact structure, fully complies with national environmental protection requirements, reduces the burden on enterprises, and is suitable for popularization and use. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] Figure 1 It is a schematic diagram of the overall process of the present invention;

[0028] Figure 2This is a schematic diagram of a high temperature incineration module of the present invention;

[0029] Figure 3 This is a schematic diagram of the rapid cooling and dioxin generation control module and the gas-solid separation module of the present invention;

[0030] Figure 4 This is a schematic diagram of the HCL separation module of the present invention;

[0031] Figure 5 This is a schematic diagram of the alkali washing and neutralization module of the present invention;

[0032] Figure 6 This is a schematic diagram of a low-temperature denitration module of the present invention;

[0033] Figure 7 This is a schematic diagram of a water treatment module of the present invention;

[0034] Figure 8 This is a schematic diagram of the molten salt cooling, transporting and packaging module of the present invention;

[0035] Fig. 9 It is a schematic diagram of the adiabatic incinerator and waste heat boiler of the present invention.

[0036] Figure: 1, waste liquid buffer tank, 2, adiabatic incinerator, 3, waste heat boiler, 4, steam drum, 5, deaerator, 6, quenching tower, 7, quenching tower replacement bin, 8, quenching water tank, 9, compressed air buffer tank, 10, bag filter (or ceramic membrane gas-solid separator), 11, bag replacement bin, 12, pre-cooling tower, 13, primary absorption tower, 14, circulating acid tank, 15, primary heat exchanger, 16, acid storage tank, 17, secondary absorption tower, 18, secondary heat exchanger, 19, high-level water tank, 20, alkali washing tower, 21, alkali liquid tank, 22, flue gas heating Heater, 23. Denitration device, 24. Denitration solution preparation tank, 25. Denitration solution buffer tank, 26. Static mixer, 27. Chimney, 28. Waste liquid booster pump, 29. Combustion-supporting fan, 30. Main combustion burner, 31. Supplementary combustion burner, 32. Double-axis cooler, 33. Water-cooled scraper slag remover, 34. Soot blowing device, 35. Boiler feed water pump, 36. Rapid cooling water pump, 37. Primary extraction pump, 38. Primary circulation pump, 39. Hydrochloric acid delivery pump, 40. Secondary circulation pump, 41. Alkali washing extraction pump, 42. Alkali washing circulation pump, 43. Flue gas heater burner, 44. Denitrification delivery pump, 45. Denitrification booster pump, 46. induced draft fan, 47. Storage tank, 48. Packing device, 201. Atomizing spray gun, 301. Salt collection chamber, 302. Rapid cooling chamber, 303. Molten salt pool, 601. Rapid cooling spray gun, 1001. Waste liquid pipeline, 1002. Natural gas pipeline, 1003. Air pipeline, 1004. Saturated steam pipeline, 1005. Desalination and deoxygenation water pipeline, 1006. Low-pressure steam pipeline, 1007. Circulating cooling water supply pipeline, 1008. Circulating Circular cooling water return pipeline, 1009, nitrogen pipeline, 1010, hydrochloric acid pipeline, 1011, compressed air pipeline, 1012, alkaline solution pipeline, 1013, denitrification feed pipeline, 1201, cooling spray gun, 1301, absorption filler layer, 1302, primary absorption nozzle, 1701, ball ring filler, 1702, secondary absorption nozzle, 1703, bubble layer, 2001, alkali washing filler layer, 2002, alkali washing spray nozzle, 2301, denitrification filler layer, 2302, denitrification nozzle, 3401, steam soot blower. DETAILED DESCRIPTION

[0037] The following will be combined with the drawings in the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0038] See also Figure 1-Figure 9The present invention provides a technical solution: comprising a high-temperature incineration module, a rapid cooling module for curbing dioxin generation, a gas-solid separation module, an HCl separation module, an alkali washing and neutralization module, a low-temperature denitration module, a water treatment module and a molten salt cooling, conveying and packaging module, wherein the high-temperature incineration module, the rapid cooling module for curbing dioxin generation, the gas-solid separation module, the HCl separation module, the alkali washing and neutralization module and the low-temperature denitration module are sequentially connected through a flue, the high-temperature incineration module comprises an adiabatic incinerator 2, wherein two layers of main burners 30 are arranged in the middle of the adiabatic incinerator 2, an atomizing spray gun 201 is installed at the upper end of the adiabatic incinerator 2, a waste liquid pipeline 1001 and a compressed air pipeline 1011 are connected to the upper outer side of the adiabatic incinerator 2, and the waste liquid pipeline 100 1 is connected to a waste liquid booster pump 28 and a waste liquid buffer tank 1 at the front end, a natural gas pipeline 1002 and an air pipeline 1003 are connected to the left side of the adiabatic boiler 2, a combustion-supporting fan 29 is connected to the air pipeline 1003, the bottom of the adiabatic incinerator 2 is connected to a waste heat boiler 3, a supplementary combustion burner 31 is installed inside the waste heat boiler 3, a soot blowing device 34 is provided on the right side of the waste heat boiler 3, a steam drum 4 is provided on the upper side of the adiabatic boiler 2, the lower end of the steam drum 4 is connected to the internal heating surface of the waste heat boiler 3 through a pipeline, a saturated steam pipeline 1004 is connected to the upper end of the steam drum 4, a desalted and deoxygenated water pipeline 1005 is connected to the right end of the steam drum 4, and a boiler feed water pump 35 is connected to the desalted and deoxygenated water pipeline 1005;

[0039] The quenching module for curbing dioxin generation includes a quenching tower 6, a quenching spray gun 601, a quenching water pump 36, and a quenching water tank 8. A quenching spray gun 601 is installed on the upper part of the quenching tower 6. The upper right end of the quenching tower 6 is connected to the quenching water tank 8 through a pipeline and the quenching water pump 36. The right end of the quenching water tank 8 is connected to a desalination and deoxygenation water pipeline 1005. The lower end of the quenching tower 6 is connected to a quenching tower replacement bin 7 through a pipeline. The right end of the quenching tower 6 is connected to a gas-solid separation module through a flue.

[0040] The gas-solid separation module includes a bag dust collector or a ceramic membrane gas-solid separator 10, and a compressed air buffer tank 9. The upper left end of the bag dust collector or the ceramic membrane gas-solid separator 10 is connected to the compressed air buffer tank 9 through a pipeline, and the right end of the compressed air buffer tank 9 is connected to a compressed air pipeline 1011. The lower end of the bag dust collector or the ceramic membrane gas-solid separator 10 is connected to a bag replacement bin 11 through a pipeline. The upper right end of the quenching tower replacement bin 7 is connected in parallel to the flue between the quenching tower 6 and the bag dust collector or the ceramic membrane gas-solid separator 10 through the flue, and the upper right end of the bag replacement bin 11 is connected in parallel to the main flue at the outlet of the bag dust collector or the ceramic membrane gas-solid separator 10 through the flue, and the lower left ends of the quenching tower replacement bin 7 and the bag replacement bin 11 are both connected to a nitrogen pipeline 1009;

[0041] The HCl separation module includes a pre-cooling tower 12, a primary absorption tower 13, a circulating acid tank 14, a heat exchanger 15, an acid storage tank 16, a secondary absorption tower 17, and a secondary heat exchanger 18. A cooling spray gun 1201 is installed at the upper end of the pre-cooling tower 12. The upper end of the pre-cooling tower 12 is connected to the primary heat exchanger 15 through a pipeline. The upper end of the heat exchanger 15 is connected to the circulating acid tank 14 through a pipeline and a primary circulation pump 38. The upper right end of the circulating acid tank 14 is connected to the acid storage tank 16 through a pipeline. The right end of the acid storage tank 16 is connected to a hydrochloric acid pipeline 1010 and a hydrochloric acid delivery pump 39. The bottom right side of the pre-cooling tower 12 is connected to the storage tank 47 at the bottom of the primary absorption tower 13 through a pipeline. The upper left end of the primary absorption tower 13 is connected to the pre-cooling tower 12 and the heat exchanger through a pipeline. On the pipeline between the heat exchangers 15, the lower right end of the primary absorption tower 13 is connected to the acid storage tank 16 and the circulating acid tank 14 respectively through a pipeline and a primary extraction pump 37, the right side of the primary absorption tower 13 is connected to the secondary absorption tower 17 through a flue, and the left side of the secondary absorption tower 17 is provided with a secondary heat exchanger 18, the lower end of the secondary heat exchanger 18 is connected to the storage tank 47 at the bottom of the secondary absorption tower 17 through a pipeline and a secondary circulation pump 40, the pipeline above the secondary circulation pump 40 is also connected to the bottom of the primary absorption tower 13, the upper end of the secondary heat exchanger 18 is connected to the middle and upper end of the secondary absorption tower 17 through a pipeline, the upper right end of the secondary absorption tower 17 is connected to the high-level water storage tank 19 through a pipeline, and the upper left end of the high-level water storage tank 19 is connected to the desalted and deoxygenated water pipeline 1005;

[0042] The alkali washing and neutralization module includes an alkali washing tower 20, the upper left end of which is connected to an alkali washing tank 21 through a pipeline and an alkali washing circulation pump 42, the right end of which is connected to an alkali solution pipeline 1012, the upper right end of which is connected to a high-level water storage tank 19 and a waste liquid buffer tank 1 through pipelines, and the upper left end of which is connected to a storage tank 47 in the alkali washing tower 20 through a pipeline and an alkali washing extraction pump 41;

[0043] The low-temperature denitration module includes a denitration device 23, a denitration solution preparation tank 24, a denitration solution buffer tank 25, a static mixer 26, and a denitration solution atomizing nozzle 2302. A flue gas heater 22 is installed on the upper end of the denitration device 23. A flue gas heater burner 43 is arranged inside the flue gas heater 22. The left end of the flue gas heater burner 43 is connected to a natural gas pipeline 1002 and an air pipeline 1003. A static mixer 26 is arranged on the right side of the denitration device 23. The right end of the static mixer 26 is connected to a desalted and deoxygenated water pipeline 1002. 05, the upper end of the static mixer 26 is connected to the denitration solution buffer tank 25 through a pipeline and a denitration solution booster pump 45, the upper right end of the denitration solution buffer tank 25 is connected to a desalting and deoxygenating water pipeline 1005, the upper left end of the denitration solution buffer tank 25 is connected to a denitration solution preparation tank 24 through a pipeline and a denitration delivery pump 44, the right end of the denitration solution preparation tank 24 is connected to a desalting and deoxygenating water pipeline 1005 and a denitration feed pipeline 1013, and the lower left end of the denitration device 23 is connected to the bottom of the chimney 27 through a flue and an induced draft fan 46;

[0044] The water treatment module includes a deaerator 5, the lower end of which is connected to a desalted and deoxygenated water pipeline 1005 on both sides, and the upper end of which is connected to a low-pressure steam pipeline 1006;

[0045] The molten salt cooling, conveying and packaging module includes a double-axis cooler 32, a water-cooled scraper slag remover 33, and a packaging device 48. The middle upper end of the water-cooled scraper slag remover 33 is connected to the double-axis cooler 32 through a pipeline, and the upper end of the double-axis cooler 32 is connected to the bottom of the waste heat boiler 3 through a pipeline. The left end of the double-axis cooler 32 is connected to a circulating cooling water supply pipeline 1007 and a circulating cooling water return pipeline 1008, and the lower end of the water-cooled scraper slag remover 33 is connected to a circulating cooling water supply pipeline 1007 and a circulating cooling water return pipeline 1008. The upper right end of the water-cooled scraper slag remover 33 is connected to the bottom of the quenching tower replacement bin 7 and the bag replacement bin 11 through pipelines, and the leftmost side of the water-cooled scraper slag remover 33 is provided with a packaging device 48;

[0046] The combustion temperature of the adiabatic incineration boiler 2 is 1200°C. The waste heat boiler 3 adopts a membrane wall type, which is composed of a salt collection chamber 301, a quenching chamber 302 and a molten salt pool 303. The salt collection chamber 301 is arranged at the lower part of the adiabatic incinerator 2. A refractory furnace wall is laid inside the membrane wall of the salt collection chamber 301. The quenching chamber 302 is composed of a membrane water-cooled wall and a water-cooled screen. A steam soot blower 3401 is arranged in the quenching chamber 302.

[0047] The first-level absorption tower 13 is made of fiberglass, and is internally provided with three layers of absorption filler layers 1301. The upper end of each absorption filler layer 1301 is provided with a first-level absorption nozzle 1302. The second-level absorption tower 17 is arranged with a ball ring filler 1701. The upper end of each ball ring filler 1701 is provided with a second-level absorption nozzle 1702. The upper end of each second-level absorption nozzle 1702 is provided with a bubble layer 1703.

[0048] The primary heat exchanger 15 and the secondary heat exchanger 18 are both graphite heat exchangers, and the left ends of the primary heat exchanger 15 and the secondary heat exchanger 18 are connected to a circulating cooling water supply pipe 1007 and a circulating cooling water return pipe 1008.

[0049] An alkali washing packing layer 2001 is provided at the upper end of the alkali washing tower 20 , and an alkali washing spray nozzle 2002 is provided at the upper end of the alkali washing packing layer 2001 .

[0050] The denitrification device 23 adopts a low-temperature denitrification method. A three-layer denitrification filler layer 2301 is provided in the middle of the denitrification device 23. A denitrification solution atomizing nozzle 2302 is provided above the denitrification filler layer 2301. The left outer end of the denitrification solution atomizing nozzle 2302 is connected to the static mixer 26 through a pipeline. An agitator is provided in the denitrification solution preparation tank 24. The denitrification agent adopts urea solution as a denitrification catalyst, and the temperature is controlled at 180~260℃.

[0051] The flue gas temperature in the quench tower 6 drops rapidly from 550° C. to 180° C. within 1 second.

[0052] Example 1: First, high-salt chlorine-containing waste liquid is sent to the high-salt chlorine-containing waste liquid buffer tank 1, and after being pressurized by the waste liquid booster pump 28, it enters the top of the adiabatic incinerator 2 and is sprayed into the adiabatic incinerator by the atomizing spray gun 201 for incineration. The waste liquid is atomized by compressed air. The adiabatic incinerator 2 is arranged with two layers of natural gas main combustion burners 30. By burning natural gas, the high-temperature incineration in the adiabatic incinerator 2 is controlled to be 1200°C. The chlorine in the high-salt chlorine-containing waste liquid is converted into HCL gas and enters the lower-level equipment-the waste heat boiler 3 with the flue gas. The waste heat boiler 3 adopts a membrane wall type and is divided into a salt collection chamber 301 and a quenching chamber 302. The salt collection chamber 301 is arranged at the lower part of the adiabatic incinerator 2. The membrane wall of the salt collection chamber 301 is laid with a refractory furnace wall to protect the membrane wall. The high-temperature molten salt from the adiabatic incinerator 2 is in the salt collection chamber 301. The salt is cooled internally and falls into the molten salt pool 303 at the bottom of the salt collecting chamber 301 and is discharged from the waste heat boiler 3; the quenching chamber 302 is composed of a membrane water-cooled wall and a water-cooled screen, and a multi-point steam soot blower 3401 is arranged in the quenching chamber 302 to blow away the ash hanging inside the quenching chamber 302. The salts in the high-salt and chlorine-containing waste liquid become molten and directly fall into the molten salt pool 303 of the waste heat boiler 3 at the bottom of the adiabatic incinerator 2. A supplementary combustion burner 31 is arranged above the molten salt pool 303. The supplementary combustion of natural gas is used to keep the molten salt in the molten salt pool 303 with good fluidity. The molten salt flows out from the salt outlet at the bottom of the molten salt pool 303 into the double-axis cooler 32, and is cooled to a solid state by circulating cooling water and discharged into the water-cooled scraper slag remover 33, and is transported to the packaging device 48 by the water-cooled scraper slag remover 33 for packaging.

[0053] The desalted water enters the deaerator 5, and is deoxygenated by introducing low-pressure steam into the deaerator 5. The deoxygenated water is sent to the steam drum 4 through the boiler feed water pump 35. The boiler water in the steam drum 4 enters the heating surface of the waste heat boiler 3 and exchanges heat with the high-temperature flue gas to generate saturated steam, which is discharged from the steam drum and sent to the factory steam network. The flue gas is rapidly cooled to 550°C in the quenching chamber 302 and is discharged from the waste heat boiler 3 and enters the quenching tower 6.

[0054] The deionized water and deoxygenated water in the quenching water tank 8 is extracted by the quenching water pump 36 to spray and cool the flue gas in the quenching tower, so that the flue gas temperature is rapidly cooled from 550°C to 180°C, thereby preventing the generation of dioxin-like harmful substances. Some solid salt particles carried by the flue gas are thrown out under the action of inertia and enter the quenching tower replacement bin 7 at the lower part of the quenching tower 6. Since the flue gas contains a large amount of HCL gas, the thrown solid salt particles also carry some HCL gas, so the solid salt particles enter the quenching tower replacement bin 7, and the HCL gas carried by the solid salt particles is replaced by nitrogen introduced into the quenching tower replacement bin 7. The HCL gas is taken out and sent back to the flue behind the quenching tower 6 by nitrogen. The solid salt particles in the quenching tower replacement bin 7 are regularly discharged and fall into the water-cooled scraper slag remover 33 at the lower part, and are transported to the packaging device 48 by the water-cooled scraper slag remover 33 for packaging.

[0055] The 180℃ low-temperature flue gas coming out of the quench tower 6 carries some solid salt particles and enters the bag filter 10. The flue gas is separated from the solid by the bag filter 10 again. The compressed air in the compressed air buffer tank 9 is used to back-blow the bags regularly to sweep the solid salt particles on the bags. The solid salt particles collected by the bag filter 10 carry some HCL gas. Therefore, a bag filter replacement bin 11 is arranged at the bottom of the bag filter 10. The bin 11 is similar to the quench tower replacement bin 7. After the HCL gas is replaced by nitrogen, the HCL gas enters the outlet flue of the bag collector 10 with the nitrogen. The collected solid salt particles are regularly discharged to the water-cooled scraper remover 33 at the bottom of the bag collector replacement bin 11, and sent to the packaging device 48 for packaging. Since the solid salt particles carried in the flue gas are all large particles of dust, the bag collector 10 can achieve a very high removal efficiency, so that the flue gas at the outlet of the bag collector 10 basically does not carry solid salt.

[0056] Taking into account the safety, durability and economy of the system, the primary absorption tower 13 is made of fiberglass. Since the flue gas temperature of 180°C at the outlet of the bag filter 10 is higher than the long-term use temperature of the fiberglass, a pre-cooling tower 12 is arranged in front of the primary absorption tower 13. The flue gas enters the pre-cooling tower 12, and the primary circulating pump 38 sprays dilute acid liquid to pre-cool the flue gas to about 80°C before entering the primary absorption tower 13. The bottom of the pre-cooling tower 12 is connected to the lower storage tank 47 of the primary absorption tower 13, and the sprayed dilute acid liquid for cooling flows into the lower storage tank 47 of the primary absorption tower 13. The primary absorption tower 13 is provided with three layers of packing layers 1301 and three layers of primary absorption nozzles 1302. The HCL gas carried in the flue gas is absorbed once by spraying a large amount of circulating dilute acid liquid. The use of a packing tower can greatly increase the contact area between the flue gas and the sprayed dilute acid liquid, thereby improving the HCL absorption efficiency. The dilute acid liquid after spraying and absorption falls into the storage tank 47 at the bottom of the primary absorption tower 13, and is extracted by the primary extraction pump 37 and sent to the circulating acid tank 14. Since the circulating dilute acid liquid will heat up after absorbing and cooling the flue gas, a primary heat exchanger 15 is provided to cool the circulating dilute acid liquid, thereby cooling the circulating dilute acid liquid from 80°C to 60°C. Subsequently, the dilute acid liquid in the circulating acid tank 14 is extracted by the primary circulating pump 38 and sent to the primary heat exchanger 15 for heat exchange. A part of the dilute acid liquid after heat exchange is sent to the pre-cooling tower 12 for spraying to pre-cool the flue gas, and the other part is sent back to the primary absorption tower 13 for circulating spraying to absorb the HCL gas. When the circulating dilute acid liquid reaches a certain concentration, the acid discharge valve is opened and a part is discharged by the primary circulating pump 38 to the acid storage tank 16 for storage. The dilute acid liquid in the acid storage tank 16 is discharged outside the boundary area through the hydrochloric acid pipeline 1010 and the hydrochloric acid delivery pump 39 for recovery treatment.

[0057] After the primary absorption tower 13 absorbs a part of the HCL gas, the 60°C flue gas enters the secondary absorption tower 17. The secondary absorption tower 17 is provided with a ball ring packing 1701. A layer of secondary absorption nozzles 1702 is arranged on the upper part of the ball ring packing 1701. The dilute acid in the lower storage tank 47 of the secondary absorption tower 17 is extracted into the spray layer through the secondary circulation pump 40 and sprayed and absorbed in the packing absorption tower. The flue gas and the circulating absorption dilute hydrochloric acid liquid move in opposite directions. The contact area between the flue gas and the dilute hydrochloric acid is increased by the ball ring packing 1701. The HCL gas in the flue gas dissolves in the dilute acid liquid, and the supersaturated water vapor condenses into water. A bubble layer 1703 is arranged on the upper part of the secondary absorption nozzle 1702, and a water film is formed on the bubble layer 1703 by supplementing 25°C industrial water. A riser is arranged in the bubble, and a rotation space is formed between the bubble and the riser. The flue gas enters the rotation space through the riser, and is sprayed from the bubble teeth at a certain speed, forming a bubbling contact with the industrial water film on the tower plate to carry out the mass transfer process. The flue gas temperature after absorption by the secondary absorption tower 17 is reduced to 50~60°C. The dilute acid liquid after absorption falls into the storage tank 47 at the bottom of the secondary absorption tower 17. Most of the dilute acid liquid is sent back to the secondary absorption tower 17 by the secondary circulation pump 40 as a spray circulation absorption liquid, and the rest is transported to the primary absorption tower 13 to replenish the liquid level. Since the temperature of the flue gas increases during the absorption of HCL gas, a secondary heat exchanger 18 is provided to cool the circulating dilute acid liquid in the secondary absorption tower to 40°C and send it back to the secondary absorption tower for spray absorption.

[0058] After the two-stage absorption tower absorbs the HCL gas, the flue gas enters the alkali washing tower 20, and the alkali solution is used to efficiently wash the flue gas. The alkali solution is prepared by sodium hydroxide and industrial water in the alkali solution tank 21. The sodium hydroxide neutralizes the residual HCL in the flue gas through the acid-base neutralization reaction, so that the acid gas emission in the flue gas meets the national standard requirements. When the sodium hydroxide alkali solution absorbs the HCL gas, sodium chloride salts will be produced and dissolved in the circulating absorption liquid. Since the front two-stage absorption tower can achieve a very high absorption efficiency for HCl gas, the amount of brine produced per hour in the alkali washing tower is greatly reduced, so the small amount of brine produced by the alkali washing tower 20 can be sent to the adiabatic incinerator 2 for incineration. When the sodium chloride salts in the circulating absorption liquid reach a certain concentration, a part of the brine is discharged to the high-salt chlorine-containing waste liquid buffer tank, and enters the adiabatic incinerator 2 with the high-salt chlorine-containing waste liquid for incineration, and the molten salt produced is collected and packaged as a by-product to achieve zero emission of the system.

[0059] The flue gas after the deacidification treatment enters the flue gas heater, and the flue gas is reheated to 220° C. by the combustion of auxiliary fuel in the flue gas heater 22 , and then enters the SCR denitrification device 23 .

[0060] The SCR denitrification device 23 adopts a low-temperature denitrification method and a low-temperature denitrification catalyst. A denitrification reducing agent is sprayed into the flue gas at a temperature of 180 to 260°C to fully mix with the flue gas. The mixed flue gas enters the low-temperature denitrification catalyst for oxidation-reduction reaction, thereby oxidizing and reducing the nitrogen oxides carried in the flue gas into nitrogen and water.

[0061] The treated flue gas meeting the 220°C standard is drawn through the induced draft fan 46 into the chimney 48 and discharged into the atmosphere.

[0062] Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that various changes, modifications, substitutions and variations may be made to the embodiments without departing from the principles and spirit of the present invention, and that the scope of the present invention is defined by the appended claims and their equivalents.

Claims

1. A zero-emission resource utilization system for high-salt and chlorine-containing organic waste liquid, comprising a high-temperature incineration module, a rapid cooling module to curb dioxin generation, a gas-solid separation module, an HCl separation module, an alkali washing and neutralization module, a low-temperature denitration module, a water treatment module, and a molten salt cooling, transportation and packaging module, wherein the high-temperature incineration module, the rapid cooling module to curb dioxin generation, the gas-solid separation module, the HCl separation module, the alkali washing and neutralization module, and the low-temperature denitration module are sequentially connected through a flue, characterized in that: The high-temperature incineration module comprises an adiabatic incinerator (2), wherein two layers of main burners (30) are arranged in the middle of the adiabatic incinerator (2), an atomizing spray gun (201) is installed at the upper end of the adiabatic incinerator (2), a waste liquid pipeline (1001) and a compressed air pipeline (1011) are connected to the upper outer part of the adiabatic incinerator (2), a waste liquid booster pump (28) and a waste liquid buffer tank (1) are connected to the front end of the waste liquid pipeline (1001), a natural gas pipeline (1002) and an air pipeline (1003) are connected to the left side of the adiabatic incinerator (2), and a combustion-supporting fan is connected to the air pipeline (1003). (29), the bottom of the adiabatic incinerator (2) is connected to a waste heat boiler (3), a supplementary combustion burner (31) is installed inside the waste heat boiler (3), a soot blowing device (34) is provided on the right side of the waste heat boiler (3), a steam drum (4) is provided on the upper side of the adiabatic incinerator (2), the lower end of the steam drum (4) is connected to the internal heating surface of the waste heat boiler (3) through a pipeline, the upper end of the steam drum (4) is connected to a saturated steam pipeline (1004), the right end of the steam drum (4) is connected to a desalting and deoxygenating water pipeline (1005), and the desalting and deoxygenating water pipeline (1005) is connected to a boiler feed water pump (35); The quenching module for curbing dioxin generation comprises a quenching tower (6), a quenching spray gun (601), a quenching water pump (36), and a quenching water tank (8). A quenching spray gun (601) is installed on the upper part of the quenching tower (6). The upper right end of the quenching tower (6) is connected to the quenching water tank (8) through a pipeline and a quenching water pump (36). The right end of the quenching water tank (8) is connected to a desalination and deoxygenation water pipeline (1005). The lower end of the quenching tower (6) is connected to a quenching tower replacement bin (7) through a pipeline. The right end of the quenching tower (6) is connected to a gas-solid separation module through a flue. The gas-solid separation module comprises a bag filter or a ceramic membrane gas-solid separator (10), and a compressed air buffer tank (9). The bag filter or the ceramic membrane gas-solid separator The upper left end of the separator (10) is connected to a compressed air buffer tank (9) through a pipeline, the right end of the compressed air buffer tank (9) is connected to a compressed air pipeline (1011), the lower end of the bag filter or the ceramic membrane gas-solid separator (10) is connected to a bag replacement bin (11) through a pipeline, the upper right end of the quench tower replacement bin (7) is connected in parallel to the flue between the quench tower (6) and the bag filter or the ceramic membrane gas-solid separator (10) through a flue, the upper right end of the bag replacement bin (11) is connected in parallel to the main flue at the outlet of the bag filter or the ceramic membrane gas-solid separator (10) through a flue, and the lower left ends of the quench tower replacement bin (7) and the bag replacement bin (11) are both connected to a nitrogen pipeline (1009); The HCl separation module comprises a pre-cooling tower (12), a primary absorption tower (13), a circulating acid tank (14), a primary heat exchanger (15), an acid storage tank (16), a secondary absorption tower (17), and a secondary heat exchanger (18). A cooling spray gun (1201) is installed at the upper end of the pre-cooling tower (12). The upper end of the pre-cooling tower (12) is connected to the primary heat exchanger (15) via a pipeline. The upper end of the primary heat exchanger (15) is connected to the circulating acid tank (14) via a pipeline and a primary circulation pump (38). The upper right end of the circulating acid tank (14) is connected to the acid storage tank (16) via a pipeline. The right end of the acid storage tank (16) is connected to a hydrochloric acid pipeline (1010) and a hydrochloric acid delivery pump (39). The bottom right side of the pre-cooling tower (12) is connected to a storage tank (47) at the bottom of the primary absorption tower (13) via a pipeline. The upper left end of the primary absorption tower (13) is connected to the pre-cooling tower (14) via a pipeline. 2) on the pipeline between the primary absorption tower (13) and the primary heat exchanger (15), the lower right end of the primary absorption tower (13) is connected to the acid storage tank (16) and the circulating acid tank (14) respectively through a pipeline and a primary extraction pump (37), the right side of the primary absorption tower (13) is connected to the secondary absorption tower (17) through a flue, the left side of the secondary absorption tower (17) is provided with a secondary heat exchanger (18), the lower end of the secondary heat exchanger (18) is connected to the storage tank (47) at the bottom end of the secondary absorption tower (17) through a pipeline and a secondary circulation pump (40), the pipeline above the secondary circulation pump (40) is also connected to the bottom of the primary absorption tower (13), the upper end of the secondary heat exchanger (18) is connected to the middle and upper end of the secondary absorption tower (17) through a pipeline, the upper right end of the secondary absorption tower (17) is connected to a high-position water storage tank (19) through a pipeline, and the upper left end of the high-position water storage tank (19) is connected to a desalted and deoxygenated water pipeline (1005); The alkali washing and neutralization module comprises an alkali washing tower (20), wherein the upper left end of the alkali washing tower (20) is connected to an alkali washing tank (21) through a pipeline and an alkali washing circulation pump (42), the right end of the alkali washing tank (21) is connected to an alkali solution pipeline (1012), the upper right end of the alkali washing tank (21) is respectively connected to a high-level water storage tank (19) and a waste liquid buffer tank (1) through pipelines, and the upper left end of the alkali washing tank (21) is connected to a storage tank (47) in the alkali washing tower (20) through a pipeline and an alkali washing extraction pump (41); the low-temperature denitration module comprises a denitration device (23), a denitration solution preparation tank (24), a denitration solution buffer tank (25), a static mixer (26), and a denitration solution atomizing nozzle (2302), the upper end of the denitration device (23) is equipped with a flue gas heater (22), the flue gas heater (22) is provided with a flue gas heater burner (43), and the flue gas heater burner (43) is provided with a flue gas heater burner (43) The left end of the burner (43) is connected to a natural gas pipeline (1002) and an air pipeline (1003); a static mixer (26) is provided on the right side of the denitration device (23); a desalination and deoxygenation water pipeline (1005) is connected to the right end of the static mixer (26); the upper end of the static mixer (26) is connected to a denitration solution buffer tank (25) through a pipeline and a denitration solution booster pump (45); the upper right end of the denitration solution buffer tank (25) is connected to a desalination and deoxygenation water pipeline (1005); the upper left end of the denitration solution buffer tank (25) is connected to a denitration solution preparation tank (24) through a pipeline and a denitration delivery pump (44); the right end of the denitration solution preparation tank (24) is connected to a desalination and deoxygenation water pipeline (1005) and a denitration feed pipeline (1013); the lower left end of the denitration device (23) is connected to the bottom of a chimney (27) through a flue and an induced draft fan (46); The water treatment module comprises a deaerator (5), the left and right sides of the lower end of the deaerator (5) are connected to desalting and deoxygenating water pipelines (1005), and the upper end of the deaerator (5) is connected to a low-pressure steam pipeline (1006); the molten salt cooling, transporting and packaging module comprises a double-axis cooler (32), a water-cooled scraper slag remover (33), and a packaging device (48), the middle upper end of the water-cooled scraper slag remover (33) is connected to the double-axis cooler (32) through a pipeline, and the upper end of the double-axis cooler (32) is connected to the bottom of the waste heat boiler (3) through a pipeline. The left end of the double-axis cooler (32) is connected to a circulating cooling water supply pipe (1007) and a circulating cooling water return pipe (1008); the lower end of the water-cooled scraper slag remover (33) is connected to a circulating cooling water supply pipe (1007) and a circulating cooling water return pipe (1008); the upper right end of the water-cooled scraper slag remover (33) is connected to the bottom of the quenching tower replacement bin (7) and the bag replacement bin (11) through pipes respectively; and the leftmost side of the water-cooled scraper slag remover (33) is provided with a packaging device (48); The combustion temperature of the adiabatic incinerator (2) is 1200° C. The waste heat boiler (3) adopts a membrane wall type and is composed of a salt collecting chamber (301), a quenching chamber (302) and a molten salt pool (303). The salt collecting chamber (301) is arranged at the lower part of the adiabatic incinerator (2). A refractory furnace wall is laid inside the membrane wall of the salt collecting chamber (301). The quenching chamber (302) is composed of a membrane water-cooled wall and a water-cooled screen. A steam soot blower (3401) is arranged in the quenching chamber (302); The primary absorption tower (13) is made of glass fiber reinforced plastics. Three layers of absorption filler layers (1301) are arranged inside the primary absorption tower (13). A primary absorption nozzle (1302) is arranged at the upper end of each absorption filler layer (1301). Ball ring fillers (1701) are arranged inside the secondary absorption tower (17). A secondary absorption nozzle (1702) is arranged at the upper end of each ball ring filler (1701). A bubble layer (1703) is arranged at the upper end of each secondary absorption nozzle (1702).

2. A zero-discharge resource utilization system for high-salt and chlorine-containing organic waste liquid according to claim 1, characterized in that: The primary heat exchanger (15) and the secondary heat exchanger (18) are both graphite heat exchangers, and the left ends of the primary heat exchanger (15) and the secondary heat exchanger (18) are both connected to a circulating cooling water supply pipe (1007) and a circulating cooling water return pipe (1008).

3. A zero-discharge resource utilization system for high-salt and chlorine-containing organic waste liquid according to claim 1, characterized in that: An alkali washing packing layer (2001) is provided at the upper end of the alkali washing tower (20), and an alkali washing spray nozzle (2002) is provided at the upper end of the alkali washing packing layer (2001).

4. A zero-discharge resource utilization system for high-salt and chlorine-containing organic waste liquid according to claim 1, characterized in that: The denitration device (23) adopts a low-temperature denitration method. A three-layer denitration filler layer (2301) is provided in the middle of the denitration device (23). A denitration solution atomizing nozzle (2302) is provided above the denitration filler layer (2301). The left outer end of the denitration solution atomizing nozzle (2302) is connected to a static mixer (26) through a pipeline. An agitator is provided in the denitration solution preparation tank (24). The denitration agent adopts urea solution as a denitration catalyst, and the temperature is controlled at 180 to 260°C.

5. A zero-discharge resource utilization system for high-salt and chlorine-containing organic waste liquid according to claim 1, characterized in that: The flue gas temperature in the quenching tower (6) drops rapidly from 550° C. to 180° C. within 1 second.

Images