NL2029607B1 - Method for co-processing combustible hazardous waste and high-salt hazardous waste - Google Patents
Method for co-processing combustible hazardous waste and high-salt hazardous waste Download PDFInfo
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- NL2029607B1 NL2029607B1 NL2029607A NL2029607A NL2029607B1 NL 2029607 B1 NL2029607 B1 NL 2029607B1 NL 2029607 A NL2029607 A NL 2029607A NL 2029607 A NL2029607 A NL 2029607A NL 2029607 B1 NL2029607 B1 NL 2029607B1
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/006—General arrangement of incineration plant, e.g. flow sheets
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Abstract
The present disclosure belongs to the technical field of resources and environment, and in particular relates to a method for co-processing combustible hazardous waste and high-salt hazardous waste. The present disclosure utilizes the high-temperature flue gas generated by the incineration of combustible hazardous waste to decompose the organic matter in the hi gh-salt hazardous waste, and can realize the co-processing of combustible hazardous waste and high-salt hazardous waste; the present disclosure co-processes combustible hazardous waste and high-salt hazardous waste, effectively utilizes the heat of hazardous waste incineration, reduces the energy consumption of high-salt hazardous waste disposal, and meanwhilee utilizes the waste residue generated in the process of hazardous waste treatment, reduces the generation of secondary hazardous waste, and reduces comprehensive disposal cost of the two types of hazardous waste. In the method of the present disclosure, the waste salt produced by decomposing organic matter can be refined to produce commercial inorganic salt, the value of the resource product is high, and it has significant economic and environmental benefits.
Description
METHOD FOR CO-PROCESSING COMBUSTIBLE HAZARDOUS WASTE
AND HIGH-SALT HAZARDOUS WASTE
[01] The present disclosure relates to the technical field of resources and environment, in particular to a method for co-processing combustible hazardous waste and high-salt hazardous waste.
[02] The amount of hazardous waste produced in China is huge every year, including more than 15 million tons of combustible hazardous wastes, more than 10 million tons of solid hazardous wastes containing inorganic salts, and more than 30 million tons of high-salt and high-organic waste water. Although this part of hazardous waste is treated in various ways such as incineration, landfill or advanced oxidation, these treatment methods generally have problems of high disposal costs and incomplete disposal, and at the same time bring a huge burden to the ecological environment.
[03] The existing combustible hazardous waste incineration processes in China generally use rotary kiln combined incineration technology. Hazardous solid waste enters the rotary kiln incinerator system through an automatic feeding device for treatment, and the solid waste is injected through pressurized atomization or screw conveying into the incinerator system for high-temperature oxidation and combustion, and the exhaust gas is sent into the secondary combustion chamber. After 1100°C high temperature oxidation, the dioxin and other organic matter are completely decomposed.
The high-temperature flue gas after incineration is discharged after the waste heat utilization and the purification of the exhaust gas supporting facilities. At the same time, the exhaust gas emission meets the National Environmental Protection Agency's "Hazardous Waste Incineration Pollution Control Standard", and finally achieves the goal of reducing, harmless and recycling waste disposal. However, existing hazardous waste Incineration systems generally have problems such as low thermal energy utilization, high operating costs, new hazardous waste generation, and unsuitable disposal of hazardous waste containing more than 3% inorganic salts.
[04] The existing high-salt hazardous waste treatment methods are mainly landfills, which occupy a large amount of land, are costly and have potential risks. Moreover, the existing method decomposes the organic matter in the high-salt hazardous waste under high temperature conditions, and the process of realizing the harmlessness and resource utilization of the high-salt hazardous waste requires more heat; in addition, due to the melting or decomposition of many inorganic salts at high temperature, inorganic salt slags on the furnace wall of the existing hazardous waste incinerator, which will corrode refractory materials or decompose to produce a large amount of corrosive gas, causing the incinerator to fail to operate normally.
[05] The purpose of the present disclosure is to provide a method for co-processing combustible hazardous waste and high-salt hazardous waste, which can realize the co- processing of combustible waste and high-salt hazardous waste, with low comprehensive cost and no new hazardous waste. Resource-based products have high value.
[06] In order to achieve the above-mentioned purpose of the present disclosure, the present disclosure provides the following technical solutions:
[07] The present disclosure provides a method for co-processing combustible hazardous waste and high-salt hazardous waste, which comprises the following steps:
[08] Incinerating combustible hazardous waste to produce flue gas and incineration exhaust gas;
[09] Using the flue gas to carbonize high-salt hazardous waste to obtain carbonized waste salt and carbonized exhaust gas;
[10] Using the flue gas to oxidize the carbonized waste salt to obtain oxidized waste salt and oxidized exhaust gas; the oxidized exhaust gas is conveyed to the carbonizing step to carbonize the high-salt hazardous waste;
[11] Dissolving, filtering, cooling and crystallization, separating and drying the said waste oxidation salt in sequence to obtain inorganic salt;
[12] Secondary combusting the incineration exhaust gas and the carbonized exhaust gas , and then post-processing the obtained flue gas.
[13] Preferably, the combustible hazardous waste comprises waste organic solvents, kettle residues or tar.
[14] Preferably, the high-salt hazardous waste is a waste containing more than 3 wt% of inorganic salt.
[15] Preferably, the temperature of the flue gas is 900 to 1100 °C.
[16] Preferably, a carbonizing temperature is 300-650 °C, and the time is 2-20s.
[17] Preferably, an oxidizing temperature is 700-1100°C, and a time is 20s~1.5h Preferably, mother liquor obtained from the crystallization is returned to the dissolving step to dissolve the waste oxidation salt.
[18] Preferably, the temperature of the secondary combustion is 1100-1300 °C, and the time is 2s~4s.
[19] Preferably, the post-treatment comprises sequentially performing waste heat utilization, quenching, primary adsorption, dust removal, deacidification, secondary adsorption and discharge of the flue gas obtained from the secondary combustion.
[20] Preferably, the method further comprising mixing the non-combustible waste residue generated in incineration step and the insoluble matter generated in filtration step, molding and sintering in turn to obtain sintered brick or ceramsite for construction.
[21] The present disclosure provides a method for co-processing combustible hazardous wastes and high-salt hazardous wastes. The present disclosure uses high- temperature flue gas generated by incineration of combustible hazardous wastes to decompose organic matter in high-salt hazardous wastes, and can realize the joint treatment of combustible hazardous wastes and high salt hazardous wastes;;
[22] The present disclosure co-processes combustible hazardous waste and high-salt hazardous waste, reduces the energy consumption of high-salt hazardous waste disposal, and at the same time utilizes the waste residue generated in the process of processing hazardous waste as resources, reduces the generation of secondary hazardous waste, and reduces the comprehensive disposal cost of the two types of hazardous waste;
[23] Inthe method of the present disclosure, the waste salt produced by decomposing organic matter can be refined to produce commercial inorganic salt, and the resource- based product has high value, which has significant economic and environmental benefits.
[24] Figure 1 is a flow chart of the method for co-processing combustible hazardous waste and high-salt hazardous waste according to the present disclosure.
[25] The present disclosure provides a method for co-processing combustible hazardous waste and high-salt hazardous waste, which includes the following steps:
[26] Incinerating combustible hazardous waste to produce flue gas and incineration exhaust gas;
[27] Using the flue gas to carbonize high-salt hazardous waste to obtain carbonized waste salt and carbonized exhaust gas;
[28] Using the flue gas to oxidize the carbonized waste salt to obtain oxidized waste salt and oxidized exhaust gas; the oxidized exhaust gas is conveyed to the carbonizing step to carbonize the high-salt hazardous waste;
[29] Dissolving, filtering, cooling and crystallization, separating and drying the said waste oxidation salt in sequence to obtain inorganic salt;
[30] Secondary combusting the incineration exhaust gas and the carbonized exhaust gas, and then post-processing the obtained flue gas.
[31] Inthe present disclosure, combustible hazardous waste is incinerated to produce flue gas and incineration exhaust gas. In the present disclosure, the combustible hazardous waste preferably includes waste organic solvents, kettle residues or tars and other types specified in the National Hazardous Waste Catalog. In the present disclosure, the temperature of the flue gas is preferably 900 to 1100 °C. After the incineration of the present disclosure, non-combustible waste slag 1s also generated, and the treatment of 5 the generated non-combustible waste slag by the present disclosure is described in detail below.
[32] After generating flue gas and incineration exhaust gas, the present disclosure uses the flue gas to carbonize high-salt hazardous waste to obtain carbonized waste salt and carbonized exhaust gas. The present disclosure preferably firstly converts the flue gas into hot air or directly uses it to carbonize and oxidize the high-salt hazardous waste, and decompose the organic matter in the high-salt hazardous waste. In the present disclosure, the high-salt hazardous waste is preferably a waste containing more than 3wt% of inorganic salt, more preferably a solid waste containing more than 30wt% or more of soluble inorganic salt. In the present disclosure, the high-salt hazardous waste 1s preferably crushed and dried in order, and then carbonized and oxidated. The present disclosure removes the moisture and volatile components in the high-salt hazardous waste through drying, which is convenient for conveying the high-salt hazardous waste to the subsequent process for use. The present disclosure does not specifically limit the specific methods and conditions of the pulverization and drying, as long as the pulverization and drying are performed in a manner well known to those skilled in the art.
[33] In the present disclosure, the carbonization temperature is preferably 300 to 650°C, more preferably 400 to 550 °C, and the time is preferably 2 to 20 s, more preferably 10 to 15 s. In the present disclosure, it is preferred that the high-salt hazardous waste that has been dried and pretreated is conveyed to the carbonization equipment, and then the waste heat of the oxidation exhaust gas is used for carbonization. The present disclosure utilizes high-temperature carbonization to decompose the organic matter in the high-salt hazardous waste, so that the organic matter is converted into organic carbon.
[34] After obtaining carbonized waste salt and carbonized exhaust gas, the present disclosure uses the flue gas to oxidize the carbonized waste salt to obtain oxidized waste salt and oxidized exhaust gas; the oxidized exhaust gas is conveyed to the carbonization step to carbonize high-salt hazardous waste. In the present disclosure, the temperature of the oxidation is preferably 700~1100 °C, more preferably 750-850 °C; The time is preferably 20s~1.5h, more preferably 50s~0.5h. In the present disclosure, the waste heat of the oxidation exhaust gas is preferably used to carbonize the high-salt hazardous waste. In the present disclosure, it is preferable to control the oxidation time within 20s~1.5h according to the different organic matter components, so as to ensure the complete decomposition of organic matter. The present disclosure oxidizes and decomposes the organic matter in the carbonized waste salt through high temperature to produce carbon dioxide and water, and completely decompose the organic matter in the waste salt. In the present disclosure, the temperature of the obtained oxidation exhaust gas is preferably 300 to 650°C, and the oxidation exhaust gas is conveyed to the carbonization step to carbonize and decompose organic matter of the high-salt hazardous waste.
[35] After the oxidized waste salt and the oxidized exhaust gas are obtained, the present disclosure sequentially dissolves, filters, cools and crystallizes, separates, and dries the oxidized waste salt to obtain an inorganic salt. The present disclosure does not specifically limit the specific methods and conditions of the dissolution, filtration, cooling crystallization, separation, and drying, as long as the methods are well known to those skilled in the art. In the present disclosure, the insoluble matter obtained by filtration is preferably water-insoluble matter such as silicon, calcium, iron, etc., which can be used to manufacture building materials, and the specific content will be described in detail later. In the present disclosure, the mother liquor obtained from the crystallization is preferably returned to the dissolution step to dissolve the waste oxidation salt.
[36] In the present disclosure, the incineration exhaust gas and the carbonized exhaust gas are subjected to secondary combustion, and then the obtained flue gas is subjected to post-treatment. In the present disclosure, the temperature of the secondary combustion is preferably 1100~1300 °C, more preferably 1150~1250 °C, and the time is preferably 2s~4s. The present disclosure preferably completely decomposes the organic matter contained in the incineration exhaust gas and the carbonized exhaust gas that has not been completely decomposed through the secondary combustion. In the present disclosure, it is preferable to exchange heat for the combustion gas obtained from the secondary combustion to provide combustion-supporting hot air for the oxidation process of the waste salt. In the present disclosure, the secondary combustion is preferably performed in a secondary combustion chamber, and the heat exchange is preferably performed in a heat exchanger.
[37] In the present disclosure, the post-treatment preferably includes sequentially performing waste heat utilization, quenching, primary adsorption, dust removal, deacidification, secondary adsorption and discharge of the flue gas obtained from the secondary combustion. In the embodiment of the present disclosure, specifically, the flue gas obtained from the secondary combustion is first used for waste heat, and then the obtained exhaust gas is sent to the quenching process (spray quenching tower) for quenching, and the high-salt wastewater (obtained from the deacidification process) is used to cool the exhaust gas rapidly to 200~250°C within 1s; at the same time, concentrate the high-salt wastewater into salty hazardous waste and convey to the carbonization step; spray the flue gas obtained after cooling into powdered activated carbon for primary adsorption (adsorption of organic dioxin), and then the obtained flue gas is subjected to deacidification treatment after dust removal, and then the obtained exhaust gas is subjected to secondary adsorption (active carbon adsorption) to meet the discharge standards.
[38] In the present disclosure, the waste heat utilization method preferably includes:
[39] 1) The flue gas from the secondary combustion is passed through a waste heat boiler to recover steam to obtain steam, and the steam is used for evaporation; the exhaust gas from the secondary combustion is cooled to 500-550 °C after passing through the waste heat boiler to obtain the waste heat utilization exhaust gas, and the obtained exhaust gas enters the spray quenching tower for subsequent operations;
[40] 2) Pass the flue gas obtained from the secondary combustion through an air heat exchanger to obtain hot air, which serves as the combustion-supporting air for the secondary combustion chamber; the exhaust gas obtained from the secondary combustion is cooled to 500-550 °C through the heat exchanger to obtain the waste heat utilization exhaust gas, and the obtained exhaust gas enters the spray quenching tower for subsequent operations.
[41] The method of the present disclosure preferably further includes mixing, molding and sintering the non-combustible waste generated in the incineration step and the insoluble matter generated in the filtering step in order to obtain sintered bricks or ceramsites for construction. In the present disclosure, it is preferred that the non- combustible waste slag and insoluble matter (which can be mixed with general solid waste for sintering and molding) are firstly combined, and then the molding and sintering processes are sequentially performed. In the present disclosure, the non-combustible waste residue contains non-combustible components such as silicon, calcium, magnesium, iron, and inorganic salts; the general solid waste is preferably fly ash, sludge, construction waste, and other solids that can be used to produce sintered bricks material. In the present disclosure, the sintering temperature is preferably 1100 to 1300 °C, more preferably 1150 to 1250 °C. In the present disclosure, the exhaust gas produced by sintering preferably enters the deacidification process for deacidification, and the obtained exhaust gas is discharged after being treated by activated carbon adsorption to meet the standard. The present disclosure does not specifically limit the specific methods and conditions of the mixing, molding and sintering, as long as the methods are well known to those skilled in the art can be selected.
[42] Figure 1 is a flow chart of the method for co-processing combustible hazardous waste and high-salt hazardous waste in the present disclosure. It can be seen from the figure that the present disclosure incinerates combustible hazardous waste to generate flue gas, and the flue gas is used to pre-dry the waste. The treated high-salt hazardous waste is carbonized to obtain carbonized waste salt and carbonized exhaust gas; then the flue gas (or hot air obtained through heat exchange) is directly used to oxidize the carbonized waste salt to obtain oxidized waste salt and oxidized exhaust gas (The oxidized exhaust gas is conveyed to the carbonization process to carbonize the high-salt hazardous waste), the oxidized waste salt is dissolved, filtered, crystallized, separated and dried in sequence to obtain inorganic salt; the exhaust gas produced by the incineration is combined with the carbonized exhaust gas and subjected to secondary combustion, and then the obtained flue gas is used for waste heat. The obtained exhaust gas enters the quenching process. After cooling, the obtained flue gas is sprayed into powdered activated carbon to adsorb organic matter, and then the obtained flue gas is subjected to deacidification after dust removal by a dust collector. Then the obtained exhaust gas 1s adsorbed by activated carbon and discharged up to the standard; the non- combustible waste generated in the incineration step and the insoluble matter generated in the filtering step are mixed with general solid waste, and then sequentially molded and sintered to obtain sintered bricks or ceramsites.
[43] The method for co-processing combustible hazardous waste and high-salt hazardous waste provided by the present disclosure will be described in detail with reference to examples, but they should not be understood as limiting the protection scope of the present disclosure.
[44] Example 1
[45] 1) The waste methanol-ethanol mixture of combustible hazardous waste (calorific value 3650kcal/kg) is conveyed to the incinerator for incineration at 50kg/h to produce flue gas. The flue gas is subjected to heat exchange to obtain hot air (temperature 800 °C). The heated flue gas exhaust gas enters step 5); 0.5kg of non-combustible waste residue is generated per hour (the main components are insoluble solid iron oxide and calcium carbonate, go to step 6) to make building materials);
[01] 2) Select high-salt hazardous waste containing sodium sulfate (85wt% sodium sulfate, 10%wt organic content, Swt% moisture) at 300kg/h, crushed to 20 mesh by a pulverizer, and conveyed to the carbonization equipment for utilization steps 2) The flue gas is carbonized at 400 °C for 5 minutes to obtain carbonized waste salt and carbonized exhaust gas; the carbonized exhaust gas enters step 5);
[46] 3) Mix the flue gas in step 1) with the carbonized waste salt, and perform oxidation at 800°C for 20s to obtain oxidized waste salt (254kg) and oxidation exhaust gas; the oxidation exhaust gas (400 °C) enters step 2), continue to carbonize sodium sulfate and high-salt hazardous waste;
[47] 4) Dissolve, filter, cool to crystallize, separate and dry the oxidized waste salt in sequence to obtain a sodium sulfate product (252kg) that meets the national standard (GB/T 6009-2014); the mother liquor obtained from crystallization and separation is returned to the dissolution step; The filtered insoluble matter (2kg), the main components are iron, calcium, silicon and other elements, go to step 6);
[48] 5) The flue gas exhaust gas obtained in step 1) and the carbonized exhaust gas obtained in step 2) are combined and conveyed to the secondary combustion chamber, and the secondary combustion is carried out at a temperature of 1200 °C for 2s. The obtained flue gas enters the air heat exchanger for heat exchange. The secondary combustion chamber provides combustion-supporting air; the obtained exhaust gas is cooled to 550 °C through a heat exchanger, and then enters the spray quenching tower.
The flue gas is quickly cooled to 200°C by desulfurization and high-salt wastewater containing 4% sodium sulfate; the high-salt wastewater is concentrated into sodium sulfate hazardous waste and conveyed to step 2); after the flue gas is cooled, it undergoes deacidification treatment, and then adsorbed by activated carbon to meet the discharge standards;
[49] 6) Mix the non-combustible waste slag obtained in step 1) and the insoluble matter obtained in step 4) with sludge (dry weight 50 kg), and sinter at 1100°C for 30 minutes to obtain 52 kg of sintered bricks; The sintered bricks are sold as commercial products after cooling; The exhaust gas from the production of sintered bricks enters the deacidification system of step 5), and is discharged after being treated by activated carbon adsorption.
[50] Example 2 [S1] 1) Convey the residual liquid from the waste kettle of combustible hazardous waste (calorific value 5200kcal/kg) to the incinerator for incineration at 50kg/h to produce flue gas. The flue gas is subjected to heat exchange to obtain hot air (temperature 810 °C), and after heat exchange the flue gas exhaust gas enters step 5); lkg of non- combustible waste slag is produced per hour (the main components are insoluble solid alumina and silica, go to step 6) for building materials);
[52] 2) Select the high-salt hazardous waste containing sodium chloride (80wt% sodium chloride, 10%wt organic content, 10wt% moisture) at a rate of 400kg/h, crushed to 25 mesh by a grinder, and conveyed to the carbonization equipment, use step 2)
Carbonize the flue gas at 450 °C for 1 minute to obtain carbonized waste salt and carbonized exhaust gas; the carbonized exhaust gas enters step 5);
[53] 3) Mix the flue gas described in step 1) with the carbonized waste salt, and perform oxidation at 810 °C for 20 minutes to obtain oxidized waste salt (320kg) and oxidation exhaust gas; the oxidation exhaust gas is 450°C, and proceed to step 2), continue to carbonize sodium sulfate and high-salt hazardous waste;
[54] 4) Dissolve, filter cool to crystallization, separate and dry the waste oxidation salt in sequence to obtain a 99.2% sodium chloride product (317kg); the mother liquor obtained from crystallization and separation is returned to the dissolution step; the insoluble matter obtained by filtration ( 3kg), the main components are iron, calcium, silicon and other elements, go to step 6);
[55] 5) Combine and convey the flue gas exhaust gas obtained in step 1) and the carbonized exhaust gas obtained in step 2) to the secondary combustion chamber, and the secondary combustion is carried out at a temperature of 1200 °C for 2s. The obtained flue gas enters the waste heat boiler to obtain steam; After passing through the waste heat boiler, the exhaust gas is cooled to 550 °C and enters the spray quenching tower.
The high-salt wastewater containing 10% calcium chloride is used to quickly cool the flue gas to 200 °C. The high-salt wastewater is concentrated into calcium chloride hazardous waste and convey to step 2); After the flue gas is cooled down, it undergoes deacidification treatment, and then adsorbed by activated carbon to meet the discharge standards;
[56] 6) Mix the non-combustible waste slag obtained in step 1) and the insolubles obtained in step 4) with fly ash (20 kg dry) to mold, and sinter at 1150 °C for 30 minutes to obtain 23 kg of sintered ceramsite; After the sintered ceramsite is cooled, it is sold as a commodity; the exhaust gas from the production of sintered ceramsite enters the deacidification system of step 5), and is discharged after being treated by activated carbon adsorption.
[57] It can be seen from the above embodiments that the present disclosure provides a method for co-processing combustible hazardous wastes and high-salt hazardous wastes. The present disclosure uses high-temperature flue gas generated by the incineration of combustible hazardous wastes to decompose organic matter in high-salt hazardous wastes, realize the co-processing of combustible hazardous waste and high- salt hazardous waste; the present disclosure co-processes combustible hazardous waste and high-salt hazardous waste, effectively utilizes the heat of hazardous waste incineration, reduces the energy consumption of high-salt hazardous waste disposal, and simultaneously resource utilizes the waste residue produced in the process of treating hazardous waste, which reduces the generation of secondary hazardous waste and reduces the comprehensive disposal cost of the two types of hazardous waste; in the method of the present disclosure, the waste salt generated by the decomposition of organic matter can be refined to produce commercial inorganic salt. Resource-based products have high value, which has significant economic and environmental benefits.
[58] The above are only the preferred embodiments of the present disclosure. It should be pointed out that for those of ordinary skill in the art, without departing from the principle of the present disclosure, varies and modifications can be made, and these varies and modifications shall be covered within the protection scope of the present disclosure.
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| Application Number | Priority Date | Filing Date | Title |
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| NL2029607A NL2029607B1 (en) | 2021-11-03 | 2021-11-03 | Method for co-processing combustible hazardous waste and high-salt hazardous waste |
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| Application Number | Priority Date | Filing Date | Title |
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| NL2029607A NL2029607B1 (en) | 2021-11-03 | 2021-11-03 | Method for co-processing combustible hazardous waste and high-salt hazardous waste |
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| NL2029607B1 true NL2029607B1 (en) | 2023-06-02 |
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