CN112197281A

CN112197281A - Incineration process treatment system for organic waste liquid

Info

Publication number: CN112197281A
Application number: CN202010858832.2A
Authority: CN
Inventors: 陈中继; 徐明稿; 刘静; 陈聪聪; 潘业彪; 孔培君
Original assignee: Zhejiang Tiancheng Engineering Design Co ltd
Current assignee: Zhejiang Tiancheng Engineering Design Co ltd
Priority date: 2020-08-24
Filing date: 2020-08-24
Publication date: 2021-01-08
Anticipated expiration: 2040-08-24
Also published as: CN112197281B

Abstract

The invention relates to the technical field of organic waste liquid incineration, and discloses an organic waste liquid incineration process treatment system aiming at the problem that secondary pollution is easily caused after organic waste liquid incineration, wherein the treatment process comprises the following steps: the system comprises a batching kettle, an incinerator, an SNCR denitration and quenching system, a primary alkaline tower, a secondary alkaline tower, an induced draft fan and a treatment area which are connected in sequence. Through an incineration process treatment system with an optimized structure, organic waste liquid is treated in time, harmful products are removed, the materials are recycled, the treatment period is short, and the environment is protected and energy is saved; the packing area of the alkaline tower is filled with the composite adsorbent, so that the adsorption area and the contact time of the alkali liquor and the waste gas are ensured, and the absorption and purification effects of the liquid alkali on the waste gas are greatly improved; the composite sol is filled in the silica support shell, the silica support shell provides better coating and supporting functions, the composite sol complicates a fluid passing path, the adsorption capacity is increased, and the composite adsorbent with good integrity, good formability and good adsorption effect is prepared.

Description

Incineration process treatment system for organic waste liquid

Technical Field

The invention relates to the technical field of organic waste liquid incineration, in particular to an incineration process treatment system for organic waste liquid.

Background

Contain the ammonia nitrogen and do not contain the organic waste liquid of ammonia nitrogen and send to the waste liquid storage tank of tank field outside by the boundary area respectively, according to production needs through organic waste liquid pump sending to the batching cauldron, adjust data such as organic waste liquid viscosity and calorific value in the batching cauldron, then keep in organic waste liquid intermediate tank through the proportioning pump with organic waste liquid, burn after burning furnace possesses the treatment condition, carry to burn through organic waste liquid booster pump and burn to burning furnace. The incineration process is a key step for realizing component conversion in the organic waste liquid, the waste liquid and oxygen in combustion air are subjected to high-temperature oxidation reaction in an incinerator, and the components and the proportion of each component of a product are related to the temperature in the incinerator, such as: chloride is burnt, and free Cl is easily generated when the temperature is lower than 850 DEG C₂And a large amount of HCl is generated when the temperature is higher than 850 ℃; incineration at high pressure of 983 ℃ is carried out, and carbon can be considered to be completely oxidized into CO₂If below this temperature, toxic carbon monoxide is formed in part; when the flame temperature is lower than 1100 ℃, the waste liquid can not be completely decomposed, and the temperature in the furnace is selected to be higher than the value; however, the waste contains N element, and the high incineration temperature can cause NO_XRapidly increase and cause secondary pollution.

Various chemical substances are generated after incineration treatment, different process modules are required to be integrated to further convert and eliminate the incineration products, and finally, the recycling of the products or the standard emission are realized, so that the energy conservation and the environmental protection are realized. Therefore, the incineration process treatment system with optimized design module and high treatment efficiency has important significance.

Patent No. CN201821656315.1, patent name "a low concentration contains organic waste liquid of sodium salt and burns burning furnace and incineration system", the utility model relates to a low concentration contains organic waste liquid of sodium salt and burns burning furnace, burn burning chamber, first changeover portion, gas-solid separation deposit room, pi shape convection current room including combustor, vertical top. The utility model discloses still relate to the system of burning that burns including the aforesaid, still include waste liquid pump, gasifier, electrostatic precipitator, draught fan, chimney and steam pocket, burn burning furnace and connect gradually through burning exhanst gas outlet and electrostatic precipitator, draught fan and chimney.

The method has the defects that the treatment period and the treatment cost of the organic waste liquid after incineration are higher.

Disclosure of Invention

The invention provides an organic waste liquid incineration process treatment system, aiming at overcoming the problem that secondary pollution is easily caused after organic waste liquid incineration.

In order to achieve the purpose, the invention adopts the following technical scheme:

an organic waste liquid incineration process treatment system comprises the following treatment processes: the system comprises a batching kettle, an incinerator, an SNCR denitration and quenching system, a primary alkaline tower, a secondary alkaline tower, an induced draft fan and a treatment area which are connected in sequence.

The whole treatment process of the invention is as follows: (1) contain the ammonia nitrogen and do not contain the organic waste liquid of ammonia nitrogen and send to the waste liquid storage tank of tank field outside by the boundary area respectively, according to production needs through organic waste liquid pump sending to the batching cauldron, adjust data such as organic waste liquid viscosity and calorific value in the batching cauldron, then keep in organic waste liquid intermediate tank through the proportioning pump with organic waste liquid, burn after burning furnace possesses the treatment condition, carry to burn through organic waste liquid booster pump and burn to burning furnace.

(2) The waste liquid and oxygen in the combustion air are subjected to high-temperature oxidation reaction in the incinerator, and the components and the component ratio of the product are related to the temperature in the incinerator, such as: chloride is burnt, and free Cl is easily generated when the temperature is lower than 850 DEG C₂And the large amount of the raw materials is generated at the temperature higher than 850 DEG CForming HCl; incineration at high pressure of 983 ℃ is carried out, and carbon can be considered to be completely oxidized into CO₂If below this temperature, toxic carbon monoxide is formed in part; practice proves that when the flame temperature is lower than 1100 ℃, the waste liquid can not be completely decomposed, and the temperature in the furnace is selected to be higher than the value; however, the waste contains N element, and the high incineration temperature can cause NO_XRapidly increase and cause secondary pollution. The combustion temperature is determined to be 1100 ℃ by calculation and engineering experience. The incinerator adopts diesel as main fuel, and ignition considers the independent air distribution mode of LPG and compressed air. The burning temperature in the incinerator is controlled to be not lower than 1100 ℃ through the burning of the fuel, and the burning temperature is realized by increasing and decreasing the fuel and the combustion air. Burner using low NO_XType design, NO in flue gas_XThe wastewater can reach the discharge standard after further treatment. The organic waste liquid is mixed in the tank area to reach the furnace feeding standard and is sent to a waste liquid spray gun on the incinerator through a relevant pipeline. The waste liquid spray gun adopts a medium atomizing nozzle, an atomizing medium is compressed air, and the waste liquid uniformly enters a hearth in a fogdrop mode. The organic waste liquid, the salt-containing waste water and the methane are burnt in the incinerator at high temperature, and then the components of the smoke can be directly discharged: n is a radical of₂、O₂、CO₂、H₂In addition to O, there are molten NaCl, Na₂SO₄。

(3) The lower part sets up SNCR aqueous ammonia spray gun in the incinerator furnace, when throwing to burn the organic waste liquid of ammonia nitrogen and need the denitration, can throw into the aqueous ammonia and carry out the denitration. The ammonia water spray gun adopts compressed air atomization, and ensures that ammonia water uniformly enters a hearth in a droplet form. Since the concentration of commercially available ammonia water is 17%, the 17% ammonia water needs to be diluted before entering the furnace. A static mixer is arranged in front of an ammonia water spray gun at the lower section of the incinerator, the static mixer is provided with two inlets of 17% ammonia water and process water respectively, the 17% ammonia water pipeline and the process water pipeline are provided with a regulating valve and a flowmeter, and the requirement of 5% ammonia water content in the incinerator is met by regulating the feeding proportion of the 17% ammonia water and the process water.

(4) The high-temperature flue gas from the incinerator directly enters the quenching tank through a vertical quenching tank downcomer. The quenching tank adopts water circulating liquid as quenching liquid.The water circulation liquid is pumped to a quenching tank from a water washing tower through a water washing circulation pump, the quenching liquid in the quenching tank is pressurized through a quenching circulation pump and then is sent to a quencher at the outlet of the incinerator, the quenching liquid contacts with high-temperature flue gas to generate a violent heat and mass transfer process, and NaCl, Na and the like in the flue gas₂SO₄Is dissolved by the quenching liquid, and the moisture in the quenching liquid is evaporated into the flue gas.

(5) The flue gas from the quench tank contains a large amount of water vapor and trace amounts of sodium salt particles and acid gases which are not absorbed in the quench tank, in addition to non-condensable gases. The flue gas is preliminarily washed and dedusted by a Venturi deduster, and further enters a secondary alkaline washing tower for acid gas absorption and washing dedusting, and alkaline washing tower bottom liquid is pressurized by a water washing circulating pump, cooled by a heat exchanger and then serves as alkaline washing tower top circulating spray liquid, and is sent to the top of the alkaline washing tower for spraying.

(6) The flue gas after alkaline washing and absorption is sent to a wet electric dust collector for further dust removal, industrial water passes through the dust collector, and slurry collected at the bottom automatically flows to a brine tank. The alkaline washing tower brine collected by the brine tank and the slurry at the bottom of the wet electric dust collector are lifted by a brine conveying pump through regulating and controlling the pH value and are conveyed to a treatment area for treatment.

Preferably, the primary alkaline washing liquid in the primary alkaline washing tower can flow back to the quenching system, and the secondary alkaline washing liquid in the secondary alkaline washing tower can flow back to the primary alkaline washing tower.

Preferably, the secondary alkaline washing liquid can also be used for preparing 5-7% NaOH solution by mass fraction for the primary alkaline washing tower and the secondary alkaline washing tower.

The primary alkaline washing tower and the secondary alkaline washing tower are arranged, so that components in the waste gas can be fully removed, and the alkaline washing efficiency is ensured. The secondary alkaline washing liquid is used for preparing NaOH solution, so that the waste liquid after alkaline washing is recycled, the waste of resources is reduced, the cost is saved, and the method is environment-friendly and energy-saving.

Preferably, the alkaline washing tower comprises a filler area arranged inside and a sprayer arranged above the filler area, and further comprises a flue gas inlet arranged below the filler area, the sprayer is connected with an alkaline liquor inlet, and a flue gas outlet is arranged above the alkaline washing tower.

Waste gas generated by a system enters an alkaline washing tower, the waste gas enters from a flue gas inlet below a packing area, alkali liquor is sprayed out from a sprayer above the packing area, the waste gas and the alkali liquor (waste gas absorption liquid) are fully contacted on a packing of the packing area, substances which are easily dissolved in water in the waste gas are almost completely adsorbed on the alkali liquor, and HCl and Cl in the waste gas₂Acid mist, NO_XAnd NH₃And the substances react with the alkali liquor to generate harmless salts and water, thereby achieving the process of alkali washing purification. The reaction of the waste gas and the alkali liquor is completed on the filler, and the high-efficiency removal of components in the waste gas requires that the waste gas and the alkali liquor have larger contact area and longer reaction time, and requires that the filler has the advantages of high mechanical strength, corrosion resistance, high porosity, large specific surface area and the like, so that the preparation of the filler with excellent performance has a decisive effect on whether the alkali washing purification is thorough or not.

Preferably, the packing region is filled with the composite adsorbent, and the preparation steps are as follows:

(1) preparing a silica supporting shell: putting 0.08-0.12% by mass of cetrimide solution into a container, adding 26-28wt% by mass of concentrated ammonia water, stirring for 20-30min, dripping a mixture of dipropyl and tetraethyl orthosilicate at the speed of 1.0-1.2mL/min, and continuing to stir for reaction for 10-12h after dripping is finished; centrifuging after the reaction is finished, washing with absolute ethyl alcohol, and drying to obtain the cetrimide-silicon dioxide composite microspheres; ultrasonically dispersing the composite microspheres in a mixed solution of concentrated hydrochloric acid and absolute ethyl alcohol with the mass fraction of 70-85%, refluxing for 6-8h under magnetic stirring, removing cetrimide by acetone, washing with ethyl alcohol, filtering, drying the obtained product in an oven at 65-75 ℃ for 10-12h, and finally obtaining a silicon dioxide support shell;

(2) grafted silica support shell: dispersing the silica support shell into N, N-dimethylformamide, adding diphenylmethane diisocyanate, stirring and reacting for 4-6h at 60-80 ℃, adding glycidyl methacrylate, continuously stirring and reacting for 1.5-3h at 75-90 ℃, centrifuging, and washing with deionized water to obtain an activated silica support shell;

(3) preparing composite sol: mixing furfural, phenolic resin, carbon nano tubes, hydroxypropyl cellulose, alumina fibers, sodium bicarbonate and water according to a mass ratio of 8-10: 1: 0.5-1: 0.3-0.5: 0.05-0.1: 0.02-0.05: 100, uniformly stirring to obtain a mixed solution, dropwise adding ammonia water with the concentration of 0.25-0.5mol/L into the mixed solution at the speed of 5-10mL/min under the stirring condition to make the mixed solution neutral, and then reacting for 8-10h at the temperature of 65-75 ℃ to obtain composite carbon sol; mixing the composite carbon sol and silicon dioxide according to the mass ratio of 50-60: 3-5, uniformly mixing to obtain composite sol;

(4) preparing a composite adsorbent: and (3) adding the activated silica support shell obtained in the step (2) into the composite sol obtained in the step (3), stirring for 4-5h to enable the composite sol to be filled into the silica support shell to obtain a filling ball, removing the redundant composite sol, drying the filling ball at 60-80 ℃ for 20-30min, carbonizing at 450-600 ℃ to obtain a carbonized filling ball, and cleaning and drying the carbonized filling ball to obtain a finished product.

The composite adsorbent is used as a filler applied to an alkaline washing tower, an alkaline washing method is adopted to remove acid gas in organisms, chlorine, hydrogen chloride and carbon dioxide are mainly used, the alkaline washing process of the alkaline washing tower belongs to a differential contact countercurrent mode, the filler in the tower body is a basic component for gas-liquid two-phase contact, and the composite adsorbent can provide a large enough surface area, so that ascending air flow and descending alkaline liquor are continuously contacted in a filler area, the concentration of fluid in the ascending air flow is lower, and the emission requirement is met.

The composite adsorbent is prepared by preparing a silica supporting shell, the silica supporting shell has good adsorption performance and large pore adsorption capacity, the prepared silica supporting shell has an inner hollow surface and micro mesopores on the shell besides an outer surface, the adsorption surface area of the silica supporting shell can be multiplied, the adsorption capacity of the silica supporting shell is improved, the adsorption capacity of the silica supporting shell is obviously improved, but the specific surface area is increased and a wide channel is provided for the air flow to pass through due to the mesopores of a shell layer and the hollow structure of the shell layer, when the composite adsorbent is filled in purified gas or liquid in an alkaline tower, the composite adsorbent can easily penetrate through the inside of the silica supporting shell, so that the purification contact process is not sufficient; therefore, the silica support shell is used as a frame structure, the hollow part in the silica support shell is filled with the composite sol, the aerogel structure formed by drying the filled composite sol has stronger adsorption capacity, the complexity of a path for purified fluid to pass through the microspheres is improved, the contact time of the fluid and the filler is prolonged, the purification effect is finally improved, and the preparation period is shortened.

In the step (1), the specific surface area of the silica support shell is increased by synthesizing the cetrimide-silica composite microspheres and then removing the cetrimide component in the composite microspheres to form a hollow porous structure; in the step (2), the silica support shell is activated and grafted with an amino structure and an isocyanate group so as to increase the surface activity of the silica support shell and promote binding sites; the composite sol is prepared in the step (3), so that the prepared sol has a good pore-forming effect, and the specific surface area and the adsorption and purification effects of the finally prepared aerogel are improved; and (4) filling the composite sol into the silica support shell, carbonizing and shaping the composite sol, and finally preparing the composite adsorbent with good integrity, good formability and better adsorption effect.

In the preparation of the composite sol, the carbon nano tube is in a hollow tubular shape and has a pore canal with a nano size, the strength of the material can be improved on the premise of not influencing the porosity of the composite carbon sol as much as possible, the toughness of the material can be improved by the alumina fiber, and the sodium bicarbonate has better pore-forming efficiency.

Preferably, the volume ratio of the cetrimide solution, the strong ammonia water, the mixed solution of dipropyl and tetraethyl orthosilicate and the mixed solution of concentrated hydrochloric acid and anhydrous ethanol in the step (1) is 145-155: 3-5: 25-30: 100-; the volume ratio of dipropyl to tetraethyl orthosilicate in the mixed liquid of dipropyl and tetraethyl orthosilicate is 4-5: 1-1.5; the volume ratio of the concentrated hydrochloric acid to the absolute ethyl alcohol in the mixed solution of the concentrated hydrochloric acid and the absolute ethyl alcohol is 1: 90-100 parts of; in the step (2), the mass ratio of the silica supporting shell to the diphenylmethane diisocyanate to the glycidyl methacrylate is 8: 0.2-0.5: 1.2-1.6.

Preferably, the carbonization process of the filling ball in the step (4) is as follows: heating the filling ball to 450-500 ℃ at the speed of 4-6 ℃/min and keeping the temperature for 60-80 min; then the temperature is raised to 550-600 ℃ at the rate of 10-15/min for carbonization for 50-60 min.

Adopt progressively heating, the form of carbomorphism is accomplished the carbomorphism gradually, and the carbomorphism here is a process step by step, and the hole that can make the inside formation of carbomorphism aerogel is more even, improves the porosity for the carbomorphism is more abundant, promotes its adsorption efficiency, can strengthen the intensity of result again, makes the inside aperture wall of aerogel be difficult for collapsing, and the guarantor type effect is better.

Preferably, the batching kettle comprises a first batching kettle and a second batching kettle, the top of the first batching kettle and the top of the second batching kettle are respectively connected with a waste liquid barrel, an ammonia nitrogen-containing waste liquid storage tank, an ammonia nitrogen-free waste liquid storage tank and a salt-containing waste liquid storage tank, the bottoms of the first batching kettle and the second batching kettle are respectively connected with an organic waste liquid removing intermediate tank, and the top of the first batching kettle and the second batching kettle is also connected with an explosion venting tank; the first batching kettle and the second batching kettle are respectively connected with an acid adding elevated tank and an alkali adding elevated tank, the top of the acid adding elevated tank is connected with a hydrochloric acid material barrel, and the top of the alkali adding elevated tank is connected with a liquid alkali waste liquid tank.

The simple reasonable batching cauldron structure of design realizes in time supplying with of raw materials in the organic waste material, and the calorific value and the ratio of the organic waste liquid of real time monitoring in the cauldron are in time acquireed required raw materials composition according to the needs of organic waste liquid composition again, and its calorific value and ratio are in an optimal balanced state after keeping the batching in the cauldron all the time, finally with this balanced state carry go organic waste liquid intermediate tank in, prepare for subsequent fully burning of burning furnace. Adopt two batching kettles simultaneous workings, the wrong peak pump liquid makes the batching cauldron be in the pump liquid state all the time, has greatly promoted work efficiency, and this process flow simple structure, join in marriage liquid high-quality and use convenient high efficiency.

Preferably, the top of the incinerator is provided with a diesel oil connector, a liquefied gas storage connector and an organic waste liquid connector, and the side surface of the incinerator is provided with a saline wastewater connector, a primary combustion-supporting air connector, a secondary combustion-supporting air connector, a tail gas connector, an ammonia water connector and an adjusting air connector; the diesel oil connecting port is respectively connected with a diesel oil tank and a diesel oil removing booster pump which are connected in parallel; the liquefied gas storage interface is connected with a liquefied gas storage tank; the organic waste liquid connector is connected with an organic waste liquid intermediate tank.

When diesel oil is needed in the incinerator, the control valve is opened, and the diesel oil flows into the incinerator from the diesel oil tank; when the diesel oil in the incinerator is excessive, the diesel oil in the incinerator flows into the diesel oil booster pump, the diesel oil content in the incinerator can be ensured to be in the optimal content range all the time, the temperature in the incinerator is ensured to be in a stable state, and the generation of harmful substances is reduced.

Preferably, the quenching system comprises a quenching tank, the top of the quenching tank is provided with a quencher, the bottom of the quenching tank is connected with a waste brine desalting tank, the side surface of the quenching tank is connected with a quenching brine desalting tank, the quenching brine desalting tank is also connected with the side surface of the quencher, the side surface of the upper end of the quenching tank is provided with a flue gas dust remover, the side surface of the quencher is connected with a high-level water tank, and the top of the quencher is provided with a high-temperature flue gas inlet.

High-temperature flue gas from an incinerator directly enters a quenching tank through a vertical quenching tank descending pipe, the quenching tank adopts water circulation liquid as quenching liquid, the water circulation liquid is pumped to the quenching tank through a quenching circulation pump, the quenching liquid in the quenching tank is pressurized through the quenching circulation pump and then is conveyed to a quencher at the outlet of the incinerator, the quencher is in contact with the high-temperature flue gas to generate a violent heat and mass transfer process, and NaCl, Na and the like in the flue gas₂SO₄Is dissolved by the quenching liquid, and the moisture in the quenching liquid is evaporated into the flue gas. The flue gas from the quench tank contains a large amount of water vapor and trace amounts of sodium salt particles and acid gases which are not absorbed in the quench tank, in addition to non-condensable gases. The high-level water tank can also supply circulating liquid in real time according to the demand condition of the quenching liquid in the quenching tank, so that the quenching tank and the cold tank are cooledThe cooler has good cooling effect and component separation effect.

Therefore, the invention has the following beneficial effects:

(1) the incineration process treatment system for the organic waste liquid is provided, the organic waste liquid is treated in time and harmful products are removed by preparing the incineration process treatment system with an optimized structure, so that the recycling of materials is realized, the treatment period is short, and the system is environment-friendly and energy-saving;

(2) the packing area of the alkaline tower is filled with the composite adsorbent, so that the adsorption area and the contact time of the alkali liquor and the waste gas are ensured, and the absorption and purification effects of the liquid alkali on the waste gas are greatly improved;

(3) the composite sol is filled in the silica support shell, the silica support shell provides better coating and supporting functions, the composite sol complicates a fluid passing path, the adsorption capacity is increased, and the composite adsorbent with good integrity, good formability and good adsorption effect is prepared.

Drawings

FIG. 1 is a schematic diagram of a caustic tower of the present invention.

FIG. 2 is a schematic view of the batch still configuration of the present invention.

FIG. 3 is a schematic view of the structure of an incinerator according to the present invention.

FIG. 4 is a schematic diagram of the cooling system of the present invention.

In the figure: 1. a flue gas inlet; 2. a filler zone; 3. a sprayer; 4. an alkali liquor inlet; 5. a flue gas outlet; 6. a first batching kettle; 7. a second batching kettle; 8. venting the explosion tank; 9. a waste liquid barrel; 10. a storage tank for ammonia nitrogen-containing waste liquid; 11. a storage tank for ammonia nitrogen-free waste liquid; 12. a salt-containing wastewater and waste liquor storage tank; 13. a hydrochloric acid charging bucket; 14. adding an acid head tank; 15. a liquid caustic soda waste liquid tank; 16. adding alkali in an elevated tank; 17. removing an organic waste liquid intermediate tank; 18. an incinerator; 19. adjusting a wind interface; 20. an ammonia water interface; 21. a tail gas interface; 22. a secondary combustion-supporting air interface; 23. a primary combustion-supporting air interface; 24. an organic waste liquid connector; 25. a liquefied gas storage interface; 26. a diesel oil connector; 27. a salt-containing wastewater interface; 28. an organic waste liquid intermediate tank; 29. a diesel tank; 30. a diesel-removing booster pump; 31. a liquefaction gas storage tank; 32. a quenching tank; 33. a quencher; 34. a high-level water tank; 35. desalting the waste brine in a desalting tank; 36. a sharp quenching brine desalting tank; 37. a flue gas dust remover; 38. and a high-temperature flue gas inlet.

Detailed Description

The invention is further described with reference to the following detailed description and accompanying drawings.

General examples

In the embodiment shown in fig. 1-4, a system for treating organic waste liquid by incineration process comprises the following steps: the system comprises a batching kettle, an incinerator, an SNCR denitration and quenching system, a primary alkaline tower, a secondary alkaline tower, an induced draft fan and a treatment area which are connected in sequence. The primary alkaline washing liquid in the primary alkaline washing tower can flow back to the quenching system, and the secondary alkaline washing liquid in the secondary alkaline washing tower can flow back to the primary alkaline washing tower; the secondary alkaline washing liquid can also be used for preparing 5-7% NaOH solution by mass fraction for the primary alkaline washing tower and the secondary alkaline washing tower.

The alkaline washing tower comprises a filler area 2 arranged inside the alkaline washing tower, a sprayer 3 arranged above the filler area 2, and a flue gas inlet 1 arranged below the filler area 2, wherein an alkali liquor inlet 4 is connected to the sprayer 3, and a flue gas outlet 5 is arranged above the alkaline washing tower. The batching kettles comprise a first batching kettle 6 and a second batching kettle 7, the tops of the first batching kettle 6 and the second batching kettle 7 are respectively connected with a waste liquid barrel 9, an ammonia nitrogen-containing waste liquid storage tank 10, an ammonia nitrogen-free waste liquid storage tank 11 and a salt-containing waste water and waste liquid storage tank 12, the bottoms of the first batching kettle 6 and the second batching kettle 7 are respectively connected with an organic waste liquid removing intermediate tank 17, and the tops of the first batching kettle and the second batching kettle are also connected with an explosion venting tank 8; the first batching kettle 6 and the second batching kettle 7 are respectively connected with an acid adding elevated tank 14 and an alkali adding elevated tank 16, the top of the acid adding elevated tank 14 is connected with a hydrochloric acid material barrel 13, and the top of the alkali adding elevated tank 16 is connected with a liquid alkali waste liquid tank 15. The top of the incinerator 18 is provided with a diesel oil connector 26, a liquefied gas storage connector 25 and an organic waste liquid connector 24, and the side surface of the incinerator 18 is provided with a salt-containing wastewater connector 27, a primary combustion-supporting air connector 23, a secondary combustion-supporting air connector 22, a tail gas connector 21, an ammonia water connector 20 and an adjusting air connector 19; the diesel connecting port 26 is respectively connected with a diesel tank 29 and a diesel-removing booster pump 30 which are connected in parallel; the liquefied gas storage interface 25 is connected with a liquefied gas storage tank 31; the organic waste liquid connection port 24 is connected to an organic waste liquid intermediate tank 28. The quenching system includes quench tank 32, quench tank 32 top is equipped with quencher 33, quench tank 32 bottom is connected with brine waste water desalting tank 35, quench tank 32 side is connected with quench brine desalting tank 36, and quench brine desalting tank 36 still is connected with quench tank 33 side simultaneously, and quench tank 32 upper end side is equipped with flue gas dust remover 37, quench tank 33 side is connected with high-order water pitcher 34, and quench tank 33 top is equipped with high-temperature flue gas import 38.

The filler area 2 is filled with a composite adsorbent, and the preparation steps of the composite adsorbent are as follows:

(1) preparing a silica supporting shell: putting 0.08-0.12% by mass of cetrimide solution into a container, adding 26-28wt% by mass of concentrated ammonia water, stirring for 20-30min, dripping a mixture of dipropyl and tetraethyl orthosilicate at the speed of 1.0-1.2mL/min, and continuing to stir for reaction for 10-12h after dripping is finished; centrifuging after the reaction is finished, washing with absolute ethyl alcohol, and drying to obtain the cetrimide-silicon dioxide composite microspheres; ultrasonically dispersing the composite microspheres in a mixed solution of concentrated hydrochloric acid and absolute ethyl alcohol with the mass fraction of 70-85%, refluxing for 6-8h under magnetic stirring, removing cetrimide by acetone, washing with ethyl alcohol, filtering, drying the obtained product in an oven at 65-75 ℃ for 10-12h, and finally obtaining a silicon dioxide support shell; the volume ratio of the cetrimide solution, the strong ammonia water, the mixed solution of dipropyl and tetraethyl orthosilicate to the mixed solution of concentrated hydrochloric acid and absolute ethyl alcohol is 145-155: 3-5: 25-30: 100-; the volume ratio of dipropyl to tetraethyl orthosilicate in the mixed liquid of dipropyl and tetraethyl orthosilicate is 4-5: 1-1.5; the volume ratio of the concentrated hydrochloric acid to the absolute ethyl alcohol in the mixed solution of the concentrated hydrochloric acid and the absolute ethyl alcohol is 1: 90-100 parts of;

(2) grafted silica support shell: dispersing the silica support shell into N, N-dimethylformamide, adding diphenylmethane diisocyanate, stirring and reacting for 4-6h at 60-80 ℃, adding glycidyl methacrylate, continuously stirring and reacting for 1.5-3h at 75-90 ℃, centrifuging, and washing with deionized water to obtain an activated silica support shell; the mass ratio of the silica supporting shell to the diphenylmethane diisocyanate to the glycidyl methacrylate is 8: 0.2-0.5: 1.2-1.6;

(4) preparing a composite adsorbent: adding the activated silica support shell obtained in the step (2) into the composite sol obtained in the step (3), stirring for 4-5h to enable the composite sol to be filled into the silica support shell to obtain a filling ball, removing the redundant composite sol, drying the filling ball at 60-80 ℃ for 20-30min, and then heating the filling ball to 450-500 ℃ at the speed of 4-6 ℃/min and keeping the temperature for 60-80 min; then heating to 550-600 ℃ at the rate of 10-15/min, carbonizing for 50-60min to obtain carbonized filling balls, and cleaning and drying to obtain the finished product.

Example 1

In the embodiment shown in fig. 1-4, a system for treating organic waste liquid by incineration process comprises the following steps: the system comprises a batching kettle, an incinerator, an SNCR denitration and quenching system, a primary alkaline tower, a secondary alkaline tower, an induced draft fan and a treatment area which are connected in sequence. The primary alkaline washing liquid in the primary alkaline washing tower can flow back to the quenching system, and the secondary alkaline washing liquid in the secondary alkaline washing tower can flow back to the primary alkaline washing tower; the secondary alkaline washing liquid can also be used for preparing NaOH solution with the mass fraction of 6% for the primary alkaline washing tower and the secondary alkaline washing tower.

(1) preparing a silica supporting shell: placing a 0.1 mass percent cetrimide solution into a container, adding 27wt percent concentrated ammonia water, stirring for 25min, dripping a mixture of dipropyl and tetraethyl orthosilicate at a speed of 1.1mL/min, and continuing to stir for reaction for 1.1h after dripping; centrifuging after the reaction is finished, washing with absolute ethyl alcohol, and drying to obtain the cetrimide-silicon dioxide composite microspheres; ultrasonically dispersing the composite microspheres in a mixed solution of concentrated hydrochloric acid and absolute ethyl alcohol with the mass fraction of 78%, refluxing for 7 hours under magnetic stirring, removing cetrimide by using acetone, washing by using ethyl alcohol, filtering, and drying the obtained product in an oven at 70 ℃ for 11 hours to finally obtain a silicon dioxide support shell; the volume ratio of the cetrimide solution, the strong ammonia water, the mixed solution of dipropyl and tetraethyl orthosilicate to the mixed solution of concentrated hydrochloric acid and absolute ethyl alcohol is 150: 4: 28: 102, and (b); the volume ratio of dipropyl to tetraethyl orthosilicate in the mixed liquid of dipropyl and tetraethyl orthosilicate is 4.5: 1.2; the volume ratio of the concentrated hydrochloric acid to the absolute ethyl alcohol in the mixed solution of the concentrated hydrochloric acid and the absolute ethyl alcohol is 1: 95;

(2) grafted silica support shell: dispersing the silica support shell into N, N-dimethylformamide, adding diphenylmethane diisocyanate, stirring at 70 ℃ for 5 hours for reaction, adding glycidyl methacrylate, continuing stirring at 82 ℃ for reaction for 2.2 hours, centrifuging, and washing with deionized water to obtain an activated silica support shell; the mass ratio of the silica supporting shell to the diphenylmethane diisocyanate to the glycidyl methacrylate is 8: 0.35: 1.4;

(3) preparing composite sol: mixing furfural, phenolic resin, carbon nano tubes, hydroxypropyl cellulose, alumina fibers, sodium bicarbonate and water according to a mass ratio of 9: 1: 0.8: 0.4: 0.08: 0.04: 100, uniformly stirring to obtain a mixed solution, dripping ammonia water with the concentration of 0.4mol/L into the mixed solution at the speed of 8mL/min under the stirring condition to enable the mixed solution to be neutral, and then reacting for 9 hours at 70 ℃ to obtain composite carbon sol; mixing the composite carbon sol and the silicon dioxide according to the mass ratio of 55: 4, uniformly mixing to obtain composite sol;

(4) preparing a composite adsorbent: adding the activated silica support shell obtained in the step (2) into the composite sol obtained in the step (3), stirring for 4.5 hours to enable the composite sol to be filled into the silica support shell to obtain a filling ball, removing the redundant composite sol, drying the filling ball at 70 ℃ for 25min, and then heating the filling ball to 480 ℃ at the speed of 5 ℃/min and keeping the temperature for 70 min; then heating to 580 deg.C at a rate of 12/min, carbonizing for 55min to obtain carbonized filler balls, cleaning, and drying to obtain the final product.

Example 2

The difference from example 1 is that the packing region 2 is filled with a composite adsorbent, which is prepared by the following steps:

(1) preparing a silica supporting shell: placing a cetrimide solution with the mass fraction of 0.09% into a container, adding concentrated ammonia water with the mass fraction of 26.5 wt%, stirring for 22min, dripping a mixture of dipropyl and tetraethyl orthosilicate at the speed of 1.05mL/min, and continuing to stir for reaction for 10.5h after dripping is finished; centrifuging after the reaction is finished, washing with absolute ethyl alcohol, and drying to obtain the cetrimide-silicon dioxide composite microspheres; ultrasonically dispersing the composite microspheres in a mixed solution of concentrated hydrochloric acid and absolute ethyl alcohol with the mass fraction of 72%, refluxing for 6.5 hours under magnetic stirring, removing cetrimide by using acetone, washing by using ethyl alcohol, filtering, drying the obtained product in a 68 ℃ oven for 10.5 hours, and finally obtaining a silicon dioxide support shell; the volume ratio of the cetrimide solution, the strong ammonia water, the mixed solution of dipropyl and tetraethyl orthosilicate to the mixed solution of concentrated hydrochloric acid and absolute ethyl alcohol is 148: 3.5: 28: 101, a first electrode and a second electrode; the volume ratio of dipropyl to tetraethyl orthosilicate in the mixed liquid of dipropyl and tetraethyl orthosilicate is 4.2: 1.1; the volume ratio of the concentrated hydrochloric acid to the absolute ethyl alcohol in the mixed solution of the concentrated hydrochloric acid and the absolute ethyl alcohol is 1: 92;

(2) grafted silica support shell: dispersing the silica support shell into N, N-dimethylformamide, adding diphenylmethane diisocyanate, stirring and reacting for 4.5h at 65 ℃, adding glycidyl methacrylate, continuously stirring and reacting for 1.8h at 78 ℃, centrifuging, and washing with deionized water to obtain an activated silica support shell; the mass ratio of the silica supporting shell to the diphenylmethane diisocyanate to the glycidyl methacrylate is 8: 0.3: 1.4;

(3) preparing composite sol: mixing furfural, phenolic resin, carbon nano tubes, hydroxypropyl cellulose, alumina fibers, sodium bicarbonate and water according to a mass ratio of 8.5: 1: 0.6: 0.35: 0.06: 0.03: 100, uniformly stirring to obtain a mixed solution, dropwise adding ammonia water with the concentration of 0.3mol/L into the mixed solution at the speed of 6mL/min under the stirring condition to make the mixed solution neutral, and then reacting at 68 ℃ for 8.5 hours to obtain composite carbon sol; mixing the composite carbon sol and the silicon dioxide according to a mass ratio of 52: 3.5, uniformly mixing to obtain composite sol;

(4) preparing a composite adsorbent: adding the activated silica support shell obtained in the step (2) into the composite sol obtained in the step (3), stirring for 4.2 hours to enable the composite sol to be filled into the silica support shell to obtain a filling ball, removing the redundant composite sol, drying the filling ball at 65 ℃ for 22min, and then heating the filling ball to 460 ℃ at the speed of 4.5 ℃/min and keeping the temperature for 65 min; then heating to 560 ℃ at the rate of 11/min, carbonizing for 52min to obtain carbonized filler balls, and cleaning and drying to obtain the finished product.

Example 3

(1) preparing a silica supporting shell: placing a 0.11 mass percent cetrimide solution into a container, adding 27.5wt percent concentrated ammonia water, stirring for 28min, dripping a mixture of dipropyl and tetraethyl orthosilicate at a speed of 1.15mL/min, and continuing to stir for reaction for 11.5h after dripping is finished; centrifuging after the reaction is finished, washing with absolute ethyl alcohol, and drying to obtain the cetrimide-silicon dioxide composite microspheres; ultrasonically dispersing the composite microspheres in a mixed solution of concentrated hydrochloric acid and absolute ethyl alcohol with the mass fraction of 82%, refluxing for 7.5 hours under magnetic stirring, removing cetrimide by using acetone, washing by using ethyl alcohol, filtering, drying the obtained product in a 72 ℃ oven for 11.5 hours, and finally obtaining a silicon dioxide support shell; the volume ratio of the cetrimide solution, the strong ammonia water, the mixed solution of dipropyl and tetraethyl orthosilicate to the mixed solution of concentrated hydrochloric acid and absolute ethyl alcohol is 152: 4.8: 29: 104; the volume ratio of dipropyl to tetraethyl orthosilicate in the mixed liquid of dipropyl and tetraethyl orthosilicate is 4.8: 1.4; the volume ratio of the concentrated hydrochloric acid to the absolute ethyl alcohol in the mixed solution of the concentrated hydrochloric acid and the absolute ethyl alcohol is 1: 98, respectively;

(2) grafted silica support shell: dispersing the silica support shell into N, N-dimethylformamide, adding diphenylmethane diisocyanate, stirring at 75 ℃ for reaction for 5.5h, adding glycidyl methacrylate, continuing stirring at 85 ℃ for reaction for 2.5h, centrifuging, and washing with deionized water to obtain an activated silica support shell; the mass ratio of the silica supporting shell to the diphenylmethane diisocyanate to the glycidyl methacrylate is 8: 0.4: 1.5;

(3) preparing composite sol: mixing furfural, phenolic resin, carbon nano tubes, hydroxypropyl cellulose, alumina fibers, sodium bicarbonate and water according to a mass ratio of 9.5: 1: 0.8: 0.45: 0.09: 0.04: 100, uniformly stirring to obtain a mixed solution, dropwise adding ammonia water with the concentration of 0.45mol/L into the mixed solution at the speed of 9mL/min under the stirring condition to make the mixed solution neutral, and then reacting at 72 ℃ for 9.5 hours to obtain composite carbon sol; mixing the composite carbon sol and the silicon dioxide according to a mass ratio of 58: 4.5, uniformly mixing to obtain composite sol;

(4) preparing a composite adsorbent: adding the activated silica support shell obtained in the step (2) into the composite sol obtained in the step (3), stirring for 4.8 hours to enable the composite sol to be filled into the silica support shell to obtain a filling ball, removing the redundant composite sol, drying the filling ball at 75 ℃ for 28min, and then heating the filling ball to 490 ℃ at the speed of 5.5 ℃/min and keeping the temperature for 75 min; then heating to 590 ℃ at the rate of 14/min, carbonizing for 58min to obtain carbonized filler balls, and cleaning and drying to obtain the finished product.

Example 4

(1) preparing a silica supporting shell: placing a 0.08 mass percent cetrimide solution into a container, adding 28 mass percent concentrated ammonia water, stirring for 20min, dripping a mixture of dipropyl and tetraethyl orthosilicate at a speed of 1.2mL/min, and continuing to stir for reaction for 10h after dripping; centrifuging after the reaction is finished, washing with absolute ethyl alcohol, and drying to obtain the cetrimide-silicon dioxide composite microspheres; ultrasonically dispersing the composite microspheres in a mixed solution of concentrated hydrochloric acid and absolute ethyl alcohol with the mass fraction of 70%, refluxing for 8 hours under magnetic stirring, removing cetrimide by using acetone, washing by using ethyl alcohol, filtering, and drying the obtained product in a 65 ℃ oven for 12 hours to finally obtain a silicon dioxide support shell; the volume ratio of the cetrimide solution, the strong ammonia water, the mixed solution of dipropyl and tetraethyl orthosilicate to the mixed solution of concentrated hydrochloric acid and absolute ethyl alcohol is 145: 5: 25: 105; the volume ratio of dipropyl to tetraethyl orthosilicate in the mixed liquid of dipropyl and tetraethyl orthosilicate is 4-5: 1-1.5; the volume ratio of the concentrated hydrochloric acid to the absolute ethyl alcohol in the mixed solution of the concentrated hydrochloric acid and the absolute ethyl alcohol is 1: 90, respectively;

(2) grafted silica support shell: dispersing the silica support shell into N, N-dimethylformamide, adding diphenylmethane diisocyanate, stirring at 60 ℃ for reaction for 6 hours, adding glycidyl methacrylate, continuing stirring at 75 ℃ for reaction for 3 hours, centrifuging, and washing with deionized water to obtain an activated silica support shell; the mass ratio of the silica supporting shell to the diphenylmethane diisocyanate to the glycidyl methacrylate is 8: 0.2: 1.6;

(3) preparing composite sol: mixing furfural, phenolic resin, carbon nano tubes, hydroxypropyl cellulose, alumina fibers, sodium bicarbonate and water according to a mass ratio of 8: 1: 1: 0.3: 0.1: 0.05: 100, uniformly stirring to obtain a mixed solution, dropwise adding ammonia water with the concentration of 0.25-0.5mol/L into the mixed solution at the speed of 5-10mL/min under the stirring condition to make the mixed solution neutral, and then reacting for 10 hours at 65 ℃ to obtain composite carbon sol; mixing the composite carbon sol and the silicon dioxide according to the mass ratio of 50: 5, uniformly mixing to obtain composite sol;

(4) preparing a composite adsorbent: adding the activated silica support shell obtained in the step (2) into the composite sol obtained in the step (3), stirring for 4 hours to enable the composite sol to be filled into the silica support shell to obtain a filling ball, removing the redundant composite sol, drying the filling ball at 60 ℃ for 30min, and then heating the filling ball to 500 ℃ at the speed of 4 ℃/min and keeping the temperature for 60 min; then heating to 600 ℃ at the speed of 10/min, carbonizing for 50min to obtain carbonized filler balls, and cleaning and drying to obtain the finished product.

Example 5

(1) preparing a silica supporting shell: placing a 0.12 mass percent cetrimide solution into a container, adding 26 mass percent concentrated ammonia water, stirring for 30min, dripping a mixture of dipropyl and tetraethyl orthosilicate at a speed of 1.0mL/min, and continuing stirring for reaction for 12h after dripping; centrifuging after the reaction is finished, washing with absolute ethyl alcohol, and drying to obtain the cetrimide-silicon dioxide composite microspheres; ultrasonically dispersing the composite microspheres in a mixed solution of concentrated hydrochloric acid and absolute ethyl alcohol with the mass fraction of 85%, refluxing for 6 hours under magnetic stirring, removing cetrimide by using acetone, washing by using ethyl alcohol, filtering, and drying the obtained product in a 65 ℃ oven for 12 hours to finally obtain a silicon dioxide support shell; the volume ratio of the cetrimide solution, the strong ammonia water, the mixed solution of dipropyl and tetraethyl orthosilicate to the mixed solution of concentrated hydrochloric acid and absolute ethyl alcohol is 155: 3: 30: 100, respectively; the volume ratio of dipropyl to tetraethyl orthosilicate in the mixed liquid of dipropyl and tetraethyl orthosilicate is 5: 1; the volume ratio of the concentrated hydrochloric acid to the absolute ethyl alcohol in the mixed solution of the concentrated hydrochloric acid and the absolute ethyl alcohol is 1: 100, respectively;

(2) grafted silica support shell: dispersing the silica support shell into N, N-dimethylformamide, adding diphenylmethane diisocyanate, stirring at 80 ℃ for reacting for 4 hours, adding glycidyl methacrylate, continuing stirring at 90 ℃ for reacting for 1.5 hours, centrifuging, and washing with deionized water to obtain an activated silica support shell; the mass ratio of the silica supporting shell to the diphenylmethane diisocyanate to the glycidyl methacrylate is 8: 0.5: 1.2;

(3) preparing composite sol: mixing furfural, phenolic resin, carbon nano tubes, hydroxypropyl cellulose, alumina fibers, sodium bicarbonate and water according to a mass ratio of 10: 1: 0.5: 0.5: 0.05: 0.05: 100, uniformly stirring to obtain a mixed solution, dropwise adding ammonia water with the concentration of 0.5mol/L into the mixed solution at the speed of 5mL/min under the stirring condition to make the mixed solution neutral, and then reacting for 8 hours at the temperature of 75 ℃ to obtain composite carbon sol; mixing the composite carbon sol and the silicon dioxide according to a mass ratio of 60: 3, uniformly mixing to obtain composite sol;

(4) preparing a composite adsorbent: adding the activated silica support shell obtained in the step (2) into the composite sol obtained in the step (3), stirring for 5 hours to enable the composite sol to be filled into the silica support shell to obtain a filling ball, removing the redundant composite sol, drying the filling ball at 60 ℃ for 30min, and then heating the filling ball to 500 ℃ at the speed of 4 ℃/min and keeping the temperature for 60 min; then heating to 550 ℃ at the rate of 15/min, carbonizing for 60min to obtain carbonized filler balls, and cleaning and drying to obtain the finished product.

Comparative example 1 (changing the volume of the composite adsorbent filled in the packing region to an equal volume of activated carbon)

Comparative example 2 (adsorbent silica support shell)

The difference from example 1 is that the filler zone 2 is filled with a silica support shell, prepared as follows:

(2) grafted silica support shell: dispersing the silica support shell into N, N-dimethylformamide, adding diphenylmethane diisocyanate, stirring at 70 ℃ for 5 hours for reaction, adding glycidyl methacrylate, continuing stirring at 82 ℃ for reaction for 2.2 hours, centrifuging, and washing with deionized water to obtain an activated silica support shell; the mass ratio of the silica supporting shell to the diphenylmethane diisocyanate to the glycidyl methacrylate is 8: 0.35: 1.4.

comparative example 3 (the adsorbent filled in the filling region is aerogel after composite sol carbonization)

The difference from the embodiment 1 is that the filler area 2 is filled with the aerogel after carbonization of the composite sol, and the preparation steps are as follows:

(1) preparing composite sol: mixing furfural, phenolic resin, carbon nano tubes, hydroxypropyl cellulose, alumina fibers, sodium bicarbonate and water according to a mass ratio of 9: 1: 0.8: 0.4: 0.08: 0.04: 100, uniformly stirring to obtain a mixed solution, dripping ammonia water with the concentration of 0.4mol/L into the mixed solution at the speed of 8mL/min under the stirring condition to enable the mixed solution to be neutral, and then reacting for 9 hours at 70 ℃ to obtain composite carbon sol; mixing the composite carbon sol and the silicon dioxide according to the mass ratio of 55: 4, uniformly mixing to obtain composite sol;

(2) carbonizing the composite sol: drying the composite sol at 70 ℃ for 25min, and heating the composite sol to 480 ℃ at the speed of 5 ℃/min and keeping the temperature for 70 min; then the temperature is raised to 580 ℃ at the speed of 12/min for carbonization for 55min, and the aerogel after carbonization of the composite sol is obtained.

The indexes of relevant performance evaluation parameters of the incineration process treatment systems of examples 1 to 5 and comparative examples 1 to 3 are shown in Table 1.

TABLE 1 Performance evaluation indexes of various items related to incineration process treatment system

Item	CO content (mg/m) in flue gas of induced draft fan³)	NO in flue gas of induced draft fan_XContent (mg/m)³)
			Example 1	0.24	0.15
Example 2	0.23	0.16
			Example 3	0.22	0.15
Example 4	0.23	0.16
			Example 5	0.24	0.17
Comparative example 1	0.42	0.28
			Comparative example 2	0.53	0.31
Comparative example 3	0.48	0.32

And (4) conclusion: in the embodiments 1 to 4, the added components and the component contents can be only within the range of the present invention, so that the composite adsorbent with good adsorption performance can be prepared, the adsorption area and the contact time are increased, and the flue gas purified by alkali washing has low harmful substance content.

Comparative example 1 is different from example 1 in that the composite adsorbent filled in the packing region is changed to an equal volume of activated carbon; the adsorption pores of the activated carbon are in the shape of cavities, and the adsorption capacity of the activated carbon to fluids (alkaline solution and waste gas) is far lower than that of the high-efficiency adsorbent in the invention, so that the concentration of impurities in reaction products finally discharged to a treatment area is increased, and the treatment period is prolonged.

Comparative example 2 differs from example 1 in that the adsorbent is a silica support shell; because the mesoporous silica supports the mesopores of the silica shell layer of the shell and the hollow structure in the mesoporous silica shell layer, a wide channel is provided for the passing of fluid while the specific surface area is increased, the fluid (alkaline solution and waste gas) can easily pass through the inside of the mesoporous silica microspheres by being filled in the filler area, the contact time of the alkaline solution and the waste gas is shortened, the insufficient purification is realized, and the product purity is reduced.

The difference between the comparative example 3 and the example 1 is that the composite adsorbent filled in the filling region is aerogel obtained by carbonizing composite sol; the form of aerogel can damage compound carbomorphism aerogel because the extrusion of aerogel at the in-process of filling, especially after adsorbing moisture and impurity, can make the structural performance variation of compound carbomorphism aerogel, the wall around the hole easily softens under the mutual extruded effect of external force and collapses for the hole blocks up and destroys, reduces the adsorption capacity of compound carbomorphism aerogel, and the adsorption efficiency variation of adsorbent, and then reduces the adsorption effect who washes with alkaline in the purifying process.

The elements and equipment used in the invention are common elements and equipment in the field if not specified; the methods used in the present invention are conventional in the art unless otherwise specified.

The above description is only a preferred embodiment of the present invention, and is not intended to limit the present invention, and all simple modifications, alterations and equivalents of the above embodiments according to the technical spirit of the present invention are still within the protection scope of the technical solution of the present invention.

Claims

1. An organic waste liquid incineration process treatment system is characterized in that the treatment process comprises the following steps: the system comprises a batching kettle, an incinerator, an SNCR denitration and quenching system, a primary alkaline tower, a secondary alkaline tower, an induced draft fan and a treatment area which are connected in sequence.

2. The system for treating organic waste liquid by incineration process according to claim 1, wherein the primary alkaline washing liquid in the primary alkaline washing tower can flow back to the quenching system, and the secondary alkaline washing liquid in the secondary alkaline washing tower can flow back to the primary alkaline washing tower.

3. A process system for incinerating an organic waste liquid according to claim 2, wherein a secondary caustic wash is also used to prepare a 5-7% by weight NaOH solution for use in said primary caustic wash tower and said secondary caustic wash tower.

4. The incineration process treatment system of organic waste liquid according to claim 1, wherein the caustic tower comprises a packing area (2) arranged inside, a sprayer (3) arranged above the packing area (2), and a flue gas inlet (1) arranged below the packing area (2), the sprayer (3) is connected with an alkali liquor inlet (4), and a flue gas outlet (5) is arranged above the caustic tower.

5. A system for treating organic waste liquid by incineration process according to claim 4, wherein the filler zone (2) is filled with a composite adsorbent, and the preparation steps are as follows:

6. The incineration process treatment system of an organic waste liquid as claimed in claim 5, wherein the volume ratio of the cetrimide solution, the concentrated ammonia water, the mixed solution of dipropyl and tetraethyl orthosilicate and the mixed solution of concentrated hydrochloric acid and anhydrous ethanol in step (1) is 145-155: 3-5: 25-30: 100-; the volume ratio of dipropyl to tetraethyl orthosilicate in the mixed liquid of dipropyl and tetraethyl orthosilicate is 4-5: 1-1.5; the volume ratio of the concentrated hydrochloric acid to the absolute ethyl alcohol in the mixed solution of the concentrated hydrochloric acid and the absolute ethyl alcohol is 1: 90-100 parts of; in the step (2), the mass ratio of the silica supporting shell to the diphenylmethane diisocyanate to the glycidyl methacrylate is 8: 0.2-0.5: 1.2-1.6.

7. The incineration process treatment system for organic waste liquid according to claim 5, wherein the carbonization process of the filling balls in the step (4) is as follows: heating the filling ball to 450-500 ℃ at the speed of 4-6 ℃/min and keeping the temperature for 60-80 min; then the temperature is raised to 550-600 ℃ at the rate of 10-15/min for carbonization for 50-60 min.

8. The incineration process treatment system of organic waste liquid according to claim 1, wherein the batching kettle comprises a first batching kettle (6) and a second batching kettle (7), the tops of the first batching kettle (6) and the second batching kettle (7) are respectively connected with a waste liquid barrel (9), an ammonia nitrogen-containing waste liquid storage tank (10), an ammonia nitrogen-free waste liquid storage tank (11) and a salt-containing waste water and waste liquid storage tank (12), the bottoms of the first batching kettle and the second batching kettle are respectively connected with an organic waste liquid removing intermediate tank (17), and the tops of the first batching kettle and the second batching kettle are also connected with an explosion venting tank (8); the first batching kettle (6) and the second batching kettle (7) are respectively connected with an acid adding elevated tank (14) and an alkali adding elevated tank (16), the top of the acid adding elevated tank (14) is connected with a hydrochloric acid material barrel (13), and the top of the alkali adding elevated tank (16) is connected with a liquid alkali waste liquid tank (15).

9. The incineration process treatment system of organic waste liquid according to claim 1, wherein a diesel oil connector (26), a liquefied gas storage connector (25) and an organic waste liquid connector (24) are arranged at the top of the incinerator (18), and a saline wastewater connector (27), a primary combustion air connector (23), a secondary combustion air connector (22), a tail gas connector (21), an ammonia water connector (20) and an air adjusting connector (19) are arranged on the side surface of the incinerator (18); the diesel connecting port (26) is respectively connected with a diesel tank (29) and a diesel-removing booster pump (30) which are connected in parallel; the liquefied gas storage interface (25) is connected with a liquefied gas storage tank (31); the organic waste liquid connecting port (24) is connected with an organic waste liquid intermediate tank (28).

10. The organic waste liquid incineration process treatment system according to claim 1, wherein the quenching system comprises a quenching tank (32), a quencher (33) is arranged at the top of the quenching tank (32), a waste brine desalting tank (35) is connected to the bottom of the quenching tank (32), a quenching brine desalting tank (36) is connected to the side of the quenching tank (32), the quenching brine desalting tank (36) is also connected to the side of the quencher (33), a flue gas dust collector (37) is arranged on the side of the upper end of the quenching tank (32), a high-level water tank (34) is connected to the side of the quencher (33), and a high-temperature flue gas inlet (38) is arranged at the top of the quencher (33).