Coprocessing method of sulfur-containing organic matter-containing hazardous waste carnallite
Through a collaborative treatment method, including incineration to remove organic matter, waste heat recovery and dust removal, defluoro-deoxygenation to produce acid and preparation of organic acids, the problem of treatment of sulfur-containing organic matter-containing miscellaneous salt waste is solved, and resource recycling and environmental protection is achieved.
Patent Information
- Application Number
- CN202411764453.1
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2024-12-04
- Publication Date
- 2025-02-28
AI Technical Summary
The prior art is difficult to effectively treat sulfur-containing organic matter-containing miscellaneous waste, resulting in most of them being treated through landfill, waste of land and prone to secondary pollution.
A collaborative treatment method is adopted, including steps: removing organic matter through incineration, dust removal by waste heat, defluoro-deoxygenation to produce acid, preparing sodium metabisulfite and sodium sulfite, and finally recovering carbon dioxide through PSA.
It has achieved efficient removal of hazardous waste miscellaneous salts and recycling of resources, and produced high-quality sulfuric acid, sodium metabisulfite and carbon dioxide, which is in line with the national three principles of solid waste treatment, protects the environment and reduces corporate costs.
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Figure CN119528091A_ABST
Abstract
Description
Technical Field
[0001] The invention relates to the technical field of waste salt recovery, and in particular to a method for co-processing sulfur-containing and organic hazardous waste waste salts. Background Art
[0002] In current industrial production, the recycling of sulfur-containing and organic salts is a major problem that has restricted the development of enterprises. The recycling process requires not only the removal of organic matter, but also the removal of sulfur in sulfur-containing salts. At present, there is no complete set of industrial equipment to effectively solve this problem. Therefore, most of the sulfur-containing salt waste is still disposed of by landfill, which not only wastes land, but also easily causes secondary pollution and increases the operating costs of enterprises. Summary of the invention
[0003] The present invention provides a method for co-processing sulfur-containing and organic hazardous waste salts in order to solve a series of problems such as there is no reasonable recovery method for the existing sulfur-containing and organic salts, most of which are still disposed of by landfill, wasting land and easily causing secondary pollution.
[0004] The present invention is implemented by the following technologies: The present invention provides a method for co-processing sulfur-containing organic hazardous waste and miscellaneous salts, comprising the following steps: a. Remove organic matter Take the sulfur-containing organic hazardous waste salt and place it in a pool kiln and incinerate it at 1300~1350℃. The fuel in the incineration process is coal gas and the combustion aid is pure oxygen. The dry gas oxygen content in the atmosphere is controlled at 6%~10%. The generated flue gas stays in the kiln for more than 10 seconds. In the process, the organic matter in the salt is incinerated and removed, and sodium silicate is prepared in a coordinated manner. The reaction principle is: Organic matter + O2 → CO2 + H2O C+Na2SO4+3.3SiO2→Na2O·3.3SiO2+CO2+SO2 b. Waste heat recovery and dust removal The high-temperature flue gas generated in step a is passed into a multi-pass waste heat boiler to solidify the dust and recover heat. The waste heat boiler adopts a multi-pass special structure. In the first pass, the flue gas is cooled and the dust is solidified and removed from the bottom of the furnace. The inlet pressure of the multi-pass waste heat boiler is -1000 Pa, the inlet temperature is 1300°C, the temperature of the flue gas entering the boiler is controlled to be above the acid dew point and discharged from the multi-pass waste heat boiler, the outlet pressure is -1500~-2000 Pa, and the outlet temperature is 300~350°C; The dust content at the outlet of the high-temperature dust collector is 5mg / m 3 ; A defluorinating agent is sprayed into the wet flue gas discharged from the multi-pass waste heat boiler, and the flue gas and the defluorinating agent are mixed and passed into a high-temperature dust collector for dust removal, and the flue gas is discharged from the high-temperature dust collector; c. Defluorination and deoxygenation acid production The flue gas after dust removal is pressurized by the induced draft fan, the outlet pressure of the induced draft fan is 20Kpa, and enters the SO2 converter for catalytic oxidation. The inlet temperature of the SO2 converter is 400℃, and the outlet temperature of the SO2 converter is 285℃; a defluorinator is installed at the inlet of the SO2 converter, and an activated alumina defluorinator is installed in the defluorinator. SO2 is converted into SO3 in the SO2 converter and releases heat, and reacts with water to produce H2SO4. The produced H2SO4 is discharged from the bottom of the acid gas condenser and sent to the acid tank; Among them, the acid gas condenser uses air for heat exchange, and the outlet temperature is 100℃. The SO2 converter is equipped with a heat recovery device and a residual boiler. The bubble pressure of the residual boiler is 5.5MPa. The O2 content after the reaction reaches 5PPM, which realizes the purification of O2 and SO3 in the flue gas and reduces the oxygen content in the flue gas. The reaction principle is: 6HF(g)+AL2O3→2ALF3(S)+3H2O 2SO2+O2+H2O→2H2SO4 d. Preparation of sodium metabisulfite and sodium sulfite The flue gas with oxygen removed is cooled and dehydrated to a SO2 content of 15%, and then reversely washed with a sodium carbonate solution. The temperature of the coke synthesis tower is 60°C to produce sodium sulfite or sodium metabisulfite. The prepared sodium metabisulfite or sodium sulfite is high-quality sodium metabisulfite or sodium sulfite. The reaction principle is: Na2CO3+2SO2→Na2S2O5+CO2 Na2CO3+SO2→Na2SO3+CO2 e. PSA recovers carbon dioxide In step d, the CO2 content in the flue gas after SO2 is removed reaches 70%. PSA is used to recover and purify the carbon dioxide to obtain the recovered carbon dioxide. As an alternative, the flue gas can be directly utilized according to the needs of subsequent processes.
[0005] Compared with the prior art, the present invention has the following beneficial effects: The present invention provides a method for the coordinated treatment of sulfur-containing and organic hazardous waste salts, which gradually removes hazardous substances and completely recovers and step-utilizes sodium elements to prepare sodium silicate and sulfur elements to prepare sulfuric acid and sodium pyrosulfite, while obtaining high-concentration carbon dioxide gas.
[0006] The present invention effectively converts sulfur-containing and organic hazardous waste into high-quality sodium sulfite or sodium metabisulfite, which complies with the three principles of national solid waste treatment: reduction (scientific and reasonable disposal of social hazardous wastes), resource utilization (using various elements of hazardous wastes to prepare qualified products), and harmlessness (no three wastes are generated during the operation of the whole process). It not only protects the environment, creates sufficient space for enterprise development, but also brings economic benefits to society. BRIEF DESCRIPTION OF THE DRAWINGS
[0007] Figure 1 A process flow diagram of the present invention is shown. DETAILED DESCRIPTION
[0008] The specific embodiments of the present invention are described in detail below.
[0009] A method for the coordinated treatment of sulfur-containing organic hazardous waste and miscellaneous salts, such as Figure 1 As shown, the specific steps are as follows: a. Remove organic matter Take the sulfur-containing organic hazardous waste salt and place it in a pool kiln at -10pa and 1350℃ for incineration. The fuel is coal gas and the combustion aid is pure oxygen. The dry gas oxygen content in the atmosphere is controlled at 6%~10%, and the generated flue gas stays in the kiln for more than 10 seconds. b. Waste heat recovery, dust removal and separation of impurities The high-temperature flue gas generated in step a is passed into a multi-pass waste heat boiler to solidify the dust and recover heat. The inlet pressure of the multi-pass waste heat boiler is -1000 Pa, the inlet temperature is 1300°C, the outlet pressure is -1500~-2000 Pa, the outlet temperature is 300~350°C, and the multi-pass waste heat boiler is discharged when the temperature drops above the acid dew point. The outlet dust content of the high-temperature dust collector is 5mg / m 3 ; A defluorinating agent is sprayed into the wet flue gas discharged from the multi-pass waste heat boiler, and the flue gas and the defluorinating agent are mixed and passed into a high-temperature dust collector for dust removal, and the flue gas is discharged from the high-temperature dust collector; c. Defluorination and deoxygenation acid production The flue gas after dust removal is pressurized by the induced draft fan, the outlet pressure of the induced draft fan is 20Kpa, and enters the SO2 converter for catalytic oxidation. The inlet temperature of the SO2 converter is 400℃, and the outlet temperature of the SO2 converter is 285℃; a defluorinator is installed at the inlet of the SO2 converter, and an activated alumina defluorinator is installed in the defluorinator. SO2 is converted into SO3 in the SO2 converter and releases heat, and reacts with water to produce H2SO4. The produced H2SO4 is discharged from the bottom of the acid gas condenser and sent to the acid tank; Among them, the acid gas condenser uses air for heat exchange, and the outlet temperature is 100℃. The SO2 converter is equipped with a heat recovery device and a residual boiler. The bubble pressure of the residual boiler is 5.5MPa. The O2 content after the reaction reaches 5PPM, which realizes the purification of O2 and SO3 in the flue gas and reduces the oxygen content in the flue gas. d. Preparation of sodium metabisulfite and sodium sulfite The flue gas with oxygen removed is cooled and dehydrated, and the SO2 content is 15%. It is then reversely washed with sodium carbonate solution. The temperature of the coke synthesis tower is 60°C to produce sodium sulfite or sodium metabisulfite. The prepared sodium metabisulfite or sodium sulfite is high-quality sodium metabisulfite or sodium sulfite. The outlet temperature of the flue gas condensation tower is 40°C, the outlet pressure of the flue gas compressor is 60 Kpa, and the outlet temperature of the tail gas scrubber is 50°C. e. PSA recovers carbon dioxide PSA is used to recover and purify carbon dioxide. The outlet pressure of the tail gas compressor is 0.5Mpa, the purity of carbon dioxide gas is 97%, the pressure is 20Kpa, the adsorption tail gas pressure is 0.4 Mpa, and carbon dioxide is recovered.
[0010] The scope of protection claimed by the present invention is not limited to the above specific embodiments. For those skilled in the art, the present invention may have various deformations and changes. Any modifications, improvements and equivalent substitutions made within the concept and principle of the present invention should be included in the protection scope of the present invention.
Claims
1. A method for the coordinated treatment of sulfur-containing and organic hazardous waste and salts, characterized in that: The following steps are involved: a. Remove organic matter Take the sulfur-containing organic hazardous waste salt and burn it at 1300~1350℃. The fuel is coal gas and the combustion aid is pure oxygen. The dry gas oxygen content in the atmosphere is controlled at 6%~10%; b. Waste heat recovery and dust removal Passing the high-temperature flue gas generated in step a into a multi-pass waste heat boiler to solidify the dust and recover heat; A defluorinating agent is sprayed into the wet flue gas discharged from the multi-pass waste heat boiler, and the flue gas and the defluorinating agent are mixed and passed into a high-temperature dust collector for dust removal, and the flue gas is discharged from the high-temperature dust collector; c. Defluorination and deoxygenation acid production The dust-removed flue gas is pressurized by the induced draft fan and enters the SO2 converter for catalytic oxidation. SO2 is converted into SO3 in the SO2 converter and releases heat, and reacts with water to produce H2SO4. The generated H2SO4 is discharged from the bottom of the acid gas condenser and sent to the acid tank; d. Preparation of sodium metabisulfite and sodium sulfite The flue gas with oxygen removed is cooled and dehydrated to a SO2 content of 15%, and then reversely washed with sodium carbonate solution to produce sodium sulfite or sodium pyrosulfite; e. PSA recovers carbon dioxide Use PSA to recover carbon dioxide for purification.
2. The method for co-processing sulfur-containing organic hazardous waste and miscellaneous salts according to claim 1, characterized in that: In step c, a defluorinator is provided at the inlet of the SO2 converter, and a heat recovery device and a residual boiler are provided in the SO2 converter.
3. The method for co-processing sulfur-containing and organic-containing hazardous waste and salts according to claim 1, characterized in that: In step a, hazardous waste salts containing sulfur and organic substances are placed in a pool kiln for incineration, and the generated flue gas stays in the kiln for more than 10 seconds.
4. The method for co-processing sulfur-containing and organic-containing hazardous waste and salts according to claim 1, characterized in that: In step b, the dust content at the outlet of the high-temperature dust collector is 5 mg / m 3 ; The inlet pressure of the multi-pass waste heat boiler is -1000 Pa, the inlet temperature is 1300℃, the outlet pressure is -1500~-2000 Pa, and the outlet temperature is 300~350℃.
5. The method for co-processing sulfur-containing and organic-containing hazardous waste and salts according to claim 1, characterized in that: In step b, the multi-pass waste heat boiler adopts a multi-pass special structure. In the first pass, the flue gas is cooled and the dust is solidified and removed from the bottom of the furnace.
6. The method for co-processing sulfur-containing and organic-containing hazardous waste and salts according to claim 1, characterized in that: In step c, the inlet temperature of the SO2 converter is 400°C, and the outlet temperature of the SO2 converter is 285°C.