阅读说明：本技术 一种垃圾热解废气净化系统及工艺 (Garbage pyrolysis waste gas purification system and technology ) 是由 张秋林 陈建军 宁平 高连昀 李琳娜 姜曼 田仔梦 李志宇 田笑言 于 2021-08-16 设计创作，主要内容包括：本发明公开了一种垃圾热解废气净化系统及工艺,所述系统包括垃圾燃烧室、换热器Ⅰ、旋风除尘器、电集除尘复合除焦油装置、活性炭吸附塔、干法脱硫反应器、干法脱氯反应器、催化燃烧器、烟囱、换热器Ⅱ、换热器Ⅲ；所述工艺包括烟气初步净化、换热升温与燃烧净化以及换热降温与助燃空气加热步骤。垃圾热解产生的烟气分别与脱氯反应气体、催化燃烧气体、空气通过换热器进行多重换热,可充分利用不同废气中的余热,将空气加热至一定温度后进入垃圾燃烧室中对垃圾进行热解处理,达到了环保节能的目的；本发明可有效去除垃圾燃烧烟气中的污染物,如颗粒物、烟尘、二噁英、焦油、SO-(2)、HCl、及其他刺激性气体等,处理后的尾气可达标排放。(The invention discloses a waste pyrolysis waste gas purification system and a process, wherein the system comprises a waste combustion chamber, a heat exchanger I, a cyclone dust collector, an electric collection and dust removal composite tar removal device, an active carbon adsorption tower, a dry desulfurization reactor, a dry dechlorination reactor, a catalytic combustor, a chimney, a heat exchanger II and a heat exchanger III; the process comprises the steps of primary purification of flue gas, heat exchange, temperature rise, combustion purification, heat exchange, temperature reduction and combustion-supporting air heating. Flue gas generated by garbage pyrolysis is respectively removedChlorine reaction gas, catalytic combustion gas and air carry out multiple heat exchange through a heat exchanger, waste heat in different waste gases can be fully utilized, the air is heated to a certain temperature and then enters a garbage combustion chamber to carry out pyrolysis treatment on garbage, and the purposes of environmental protection and energy saving are achieved; the invention can effectively remove pollutants in the waste combustion flue gas, such as particulate matters, smoke dust, dioxin, tar and SO 2 HCl and other irritant gases, and the treated tail gas can reach the standard emission.)

1. A waste pyrolysis waste gas purification system comprises a waste combustion chamber (1), a heat exchanger I (2), a cyclone dust collector (3), an electric collection dust removal composite tar removing device (4), an active carbon adsorption tower (5), a dry desulfurization reactor (6), a dry dechlorination reactor (7), a catalytic combustor (8), a chimney (9), a heat exchanger II (10) and a heat exchanger III (11), and is characterized in that a waste combustion flue gas outlet (1-1) of the waste combustion chamber (1) is connected with a high-temperature gas inlet (2-1) of the heat exchanger I through a pipeline, a high-temperature gas outlet (2-2) of the heat exchanger I is connected with a cyclone dust collector gas inlet (3-1) of the cyclone dust collector (3) through a pipeline, and a cyclone dust collector gas outlet (3-2) is connected with a device gas inlet (4-1) of the electric collection dust removal composite tar removing device (4) through a pipeline, a gas outlet (4-2) of the device is connected with a gas inlet (5-1) of an adsorption tower of a charcoal adsorption tower (5) through a pipeline, the gas outlet (5-2) of the adsorption tower is connected with a gas inlet (6-1) of a dry desulphurization reactor of a pipeline dry desulphurization reactor (6), the gas outlet (6-2) of the dry desulphurization reactor is connected with a gas inlet (7-1) of a dry dechlorination reactor (7) through a pipeline, the gas outlet (7-2) of the dry dechlorination reactor is connected with a low-temperature gas inlet (2-3) of a heat exchanger I through a pipeline, a pipe wall outlet (1-2) is arranged at the upper end of the pipe wall of a garbage combustion chamber (1), a pipe wall inlet (1-3) is arranged at the lower end of the pipe wall, the low-temperature gas outlet (2-4) of the heat exchanger I is connected with the pipe wall inlet (1-3) through a pipeline, the pipe wall outlet (1-2) is connected with a low-temperature gas inlet (10-1) of a heat exchanger II through a pipeline, the low-temperature gas outlet (10-2) of the heat exchanger II is connected with a catalytic combustor gas inlet (8-1) of a catalytic combustor (8) through a pipeline, the catalytic combustor gas outlet (8-2) is connected with a high-temperature gas inlet (10-3) of the heat exchanger II through a pipeline, a high-temperature gas outlet (10-4) of the heat exchanger II is connected with a high-temperature gas inlet (11-1) of a heat exchanger III (11) through a pipeline, a high-temperature gas outlet (11-2) of the heat exchanger III is connected with a chimney inlet (9-1) of a chimney (9) through a pipeline, the low-temperature gas inlet (11-3) of the heat exchanger III is an air inlet, and the low-temperature gas outlet (11-4) of the heat exchanger III is respectively connected with an air inlet (1) of a garbage combustion chamber (1) of the garbage combustion chamber (1) through a pipeline 4) And a catalytic combustor air inlet (8-3) of the catalytic combustor (8) is connected.

2. The waste pyrolysis waste gas purification system according to claim 1, wherein the waste combustion chamber (1) comprises a waste room and a combustion chamber, the temperature in the combustion chamber is 700 ℃, high-temperature flue gas generated by waste pyrolysis is collected by a collector and then discharged from a waste combustion flue gas outlet (1-1), the temperature of the outlet flue gas is 170-190 ℃, and the flow rate of the flue gas is 1000-10000 m³/h。

3. The waste pyrolysis exhaust gas purification system according to claim 1, wherein the outlet flue gas temperature of the high-temperature gas outlet (2-2) of the heat exchanger I is 120-130 ℃.

4. The waste pyrolysis waste gas purification system according to claim 1, wherein the outlet gas temperature of the pipe wall outlet (1-2) is 140-160 ℃, and the outlet gas temperature of the low-temperature gas outlet (10-2) of the heat exchanger II is 170-190 ℃; the outlet gas temperature of a high-temperature gas outlet (10-4) of the heat exchanger II is 170-190 ℃; the outlet gas temperature of the high-temperature gas outlet (11-2) of the heat exchanger III is 140-150 ℃.

5. The waste pyrolysis exhaust gas purification system according to claim 1, wherein the outlet gas temperature of the gas outlet (7-2) of the dry dechlorination reactor is 50-70 ℃; the outlet gas temperature of the low-temperature gas outlet (2-4) of the heat exchanger I is 100-120 ℃.

6. The waste pyrolysis exhaust gas purification system according to claim 1, wherein the catalytic burner (8) contains a sulfur-resistant and chlorine-resistant catalyst material, and the outlet gas temperature of the catalytic burner gas outlet (8-2) is 200 to 250 ℃.

7. A process of the waste pyrolysis waste gas purification system according to any one of claims 1 to 6, characterized in that flue gas combusted in the waste combustion chamber (1) enters a heat exchanger I (2) for heat exchange and temperature reduction, and then the flue gas is sequentially treated by a cyclone dust collector (3), an electric collection and dust removal composite tar removal device (4), an activated carbon adsorption tower (5), a dry desulfurization reactor (6) and a dry dechlorination reactor (7) to obtain low-temperature primary purified gas;

the primary purified gas is subjected to heat exchange and temperature rise respectively through a heat exchanger I (2), a garbage combustion chamber (1) and a heat exchanger II (10), and then enters a catalytic combustor (8) for treatment to obtain high-temperature purified gas;

high-temperature purified gas is sent to a heat exchanger II (10) for heat exchange and temperature reduction, and then is subjected to heat exchange and temperature reduction by a heat exchanger III (11) so as to heat exchange and temperature rise of air; the purified gas after being cooled is discharged outside through a chimney (9); the air after temperature rise is sent to a garbage combustion chamber (1) and a catalytic combustor (8) to be used as combustion-supporting air.

Technical Field

The invention belongs to the technical field of waste pyrolysis waste gas purification treatment, and particularly relates to a waste pyrolysis waste gas purification system and process.

Background

The rapid development of urbanization, resource waste to improve economy, and the dilemma of surrounding garbage in more and more cities. A large amount of solid wastes generated in daily life of cities bring huge pressure to the environment, and the urban wastes can generate a large amount of harmful components in the processes of collection, transportation and treatment, so that the urban wastes pollute the atmosphere, soil, water sources and the like, and the urban garbage is one of the major environmental problems facing China. At present, the domestic municipal domestic waste treatment mainly comprises three technologies of landfill, composting and incineration. The landfill technology occupies soil, and the landfill leachate can cause serious water pollution, but the composting method has the problems of incomplete compost fermentation and easy secondary pollution because the municipal garbage in China is mainly mixed and collected, the garbage sources are wide, the components are complex and variable, and a large amount of components which cannot be fermented and degraded exist in the garbage.

In the current municipal waste treatment technology, incineration is used as a technology with low cost, good effect and high benefit, but the combined production of waste incineration and heat and power has large investment and high requirement on equipment process management, and the current waste incineration is mainly used for large-scale municipal waste treatment (the daily treatment capacity is more than 50 tons). And the garbage generation amount in remote rural towns is small, the garbage station has wide dispersion range, and the requirement of garbage incineration on scale cannot be met. The garbage pyrolysis technology can stably treat garbage under the condition of relatively low temperature without adding extra fuel, has small investment on single equipment, is more suitable for daily treatment of 5-20 tons of household garbage, and has obvious advantages in the garbage treatment of rural towns. However, there are some technical defects in the garbage pyrolysis facility, which results in the generation of a large amount of smoke, dust, carcinogenic dioxin, and harmful gases such as CO and SO during the incineration of garbage₂、NO_XCompounds of HCl and benzene cause harm to human health and affect the atmospheric environment of towns and villages.

It is known from patent search that the following patents exist for the waste incineration flue gas purification treatment technology:

patent 1: application number CN201821882519.7, this patent discloses a municipal solid waste combustion flue gas purification system, this system includes flue gas purification equipment and adsorbent regeneration facility, wherein: the flue gas purification equipment comprises a cooling device, a fly ash spraying and decontamination device, a calcium-based adsorbent spraying and desulfurization device, an activated carbon spraying and decontamination device, an induced draft fan and a bag-type dust collector which are sequentially connected; the adsorbent regeneration equipment comprises a recovery device, a regeneration device and a spraying treatment liquid decontamination device which are connected in sequence. The method can effectively remove pollutants in the flue gas through the flue gas purification equipment, wherein the fly ash collected in the bag-type dust collector is used as an adsorbent in the first step, and the pollutants are adsorbed while the wastes are recycled; in addition, the device is also provided with catalyst regeneration equipment, pollutants on the deactivated adsorbent are subjected to desorption reaction by heating to form regenerated adsorbent, and the regenerated adsorbent is sent to a fly ash spraying decontamination device for recycling, so that the production cost can be effectively reduced.

Patent 2: the application number is CN201920129294.6, and the patent provides a garbage combustion flue gas filtering device which comprises a spray tower, wherein a horizontally arranged and cylindrical filter cylinder is rotatably connected to the middle position inside the spray tower, and a plurality of filtering holes are uniformly formed in the circumferential side wall of the filter cylinder; both ends of the filter cartridge are open, and both ends of the filter cartridge are rotatably connected to the side walls of both sides of the spray tower through bearings; the filter cartridge is driven to rotate by a driving mechanism; a cleaning component used for cleaning the outer side wall of the filter cartridge is also arranged in the spray tower; the inner upper part of the spray pipe is fixedly connected with a horizontally arranged spray pipe, wherein the lower part of the spray pipe is provided with a plurality of spray heads facing the filter cartridge; the spray pipe is communicated with the water outlet end of a water pump fixedly arranged on the outer wall of the spray tower through a water guide pipe; this patent is good to the filter effect of rubbish burning flue gas, can clean the cartridge filter moreover to reduce the probability that the cartridge filter blockked up.

Patent 3: application number CN202010828280.0, which discloses a method for treating waste gas generated by low-temperature pyrolysis of household garbage, comprising the following steps: step 1, inputting the waste gas into a spraying device, and spraying the waste gas by spraying a spraying liquid to remove part of smoke dust and tar substances and part of SO₂、NO_xHF, HCl, heavy metals and dioxins and water-soluble contaminants; step 2, treating the waste gas treated by the spraying device in the step 1 by a filtering and purifying device, and removing residual pollutants in the waste gas in the filtering and purifying device by a demisting layer, a composite adsorption material layer, a biological composite material layer and an adsorption layer in sequence; and 3, monitoring the gas treated by the filtering and purifying device on line, and discharging the gas after the monitoring reaches the standard. The waste gas of this patent application is monitored through on-line monitoring system after spray set, filtration purification device handle, all accords with "domestic waste burns pollution control standard", discharge up to standard.

According to the three purification patent technologies for the waste combustion flue gas, the designed system or method can be found to involve a spraying device, the spraying device is adopted to clean the flue gas in waste incineration so as to remove acid gas or other water-soluble organic pollutants, the spraying liquid is an alkaline solution, acid-alkali liquid wastewater is easy to generate after the flue gas is treated, the subsequent treatment process is complex, and secondary pollution is easy to generate. In addition, the heat value in the flue gas cannot be effectively utilized, and the temperature of the treated and discharged flue gas is higher, so that the environment-friendly requirement is difficult to meet. According to the control requirement on the emission of waste incineration flue gas in the standard for controlling pollution of household garbage incineration (GB18485-2014), and the formal implementation of the national solid waste pollution environment control law newly revised on 9/1/2020, the waste incineration facility is required to be provided with a flue gas treatment facility, so that various pollutants in the waste incineration flue gas are ensured to be discharged up to the standard, heavy metals, organic pollutants and the like are prevented from being discharged into an environment medium, and meanwhile, if the heat and the waste gas generated by waste incineration are recycled, the purpose of recycling the waste can be achieved, and additional economic value can be created. Therefore, it is necessary to develop a waste pyrolysis exhaust gas purification system and process capable of effectively recovering heat while ensuring the flue gas purification effect.

Disclosure of Invention

The invention aims to provide a waste pyrolysis waste gas purification system.

The second purpose of the invention is to provide a process of the waste pyrolysis waste gas purification system.

The first purpose of the invention is realized by the following steps that the device comprises a garbage combustion chamber, a heat exchanger I, a cyclone dust collector, an electric collection and dust removal composite tar removal device, an active carbon adsorption tower, a dry desulfurization reactor, a dry dechlorination reactor, a catalytic combustor, a chimney, a heat exchanger II and a heat exchanger III, wherein a garbage combustion flue gas outlet of the garbage combustion chamber is connected with a high-temperature gas inlet of the heat exchanger I through a pipeline, a high-temperature gas outlet of the heat exchanger I is connected with a cyclone dust collector gas inlet of the cyclone dust collector through a pipeline, a cyclone dust collector gas outlet is connected with a device gas inlet of the electric collection and dust removal composite tar removal device through a pipeline, a device gas outlet is connected with an adsorption tower gas inlet of the active carbon adsorption tower through a pipeline, a dry desulfurization reactor gas outlet of the dry desulfurization reactor is connected with a dry desulfurization reactor gas inlet of the pipeline, and a dry desulfurization reactor gas outlet is connected with a dry dechlorination reactor gas inlet of the dry dechlorination reactor through a pipeline, the gas outlet of the dry dechlorination reactor is connected with a low-temperature gas inlet of a heat exchanger I through a pipeline, the upper end of the pipe wall of the garbage combustion chamber 1 is provided with a pipe wall outlet, the lower end of the pipe wall is provided with a pipe wall inlet, the low-temperature gas outlet of the heat exchanger I is connected with the pipe wall inlet through a pipeline, the pipe wall outlet is connected with a low-temperature gas inlet of a heat exchanger II through a pipeline, the low-temperature gas outlet of the heat exchanger II is connected with a gas inlet of a catalytic combustor of the catalytic combustor through a pipeline, the gas outlet of the catalytic combustor is connected with a high-temperature gas inlet of the heat exchanger II through a pipeline, the high-temperature gas outlet of the heat exchanger II is connected with a high-temperature gas inlet of a heat exchanger III 11 through a pipeline, the high-temperature gas outlet of the heat exchanger III is connected with a chimney inlet of a chimney through a pipeline, the low-temperature gas inlet of the heat exchanger III is an air inlet of the garbage combustion chamber through a pipeline, The catalytic burner air inlet of the catalytic burner is connected.

The second purpose of the invention is realized by that, specifically, the combustion flue gas of the garbage combustion chamber enters a heat exchanger I for heat exchange and temperature reduction, and then the flue gas is sequentially treated by a cyclone dust collector, an electric collection and dust removal composite tar removal device, an activated carbon adsorption tower, a dry desulfurization reactor and a dry dechlorination reactor to obtain low-temperature primary purified gas;

the primary purified gas is subjected to heat exchange and temperature rise respectively through a heat exchanger I, a garbage combustion chamber and a heat exchanger II, and then enters a catalytic combustor for treatment to obtain high-temperature purified gas;

high-temperature purified gas is sent to a heat exchanger II for heat exchange and cooling, and then is subjected to heat exchange and cooling by a heat exchanger III, so that the air is subjected to heat exchange and temperature rise; the purified gas after being cooled is discharged out through a chimney; and sending the air after temperature rise to a garbage combustion chamber and a catalytic combustor to be used as combustion-supporting air.

Compared with the prior art, the invention has the following technical effects:

1. flue gas generated by pyrolysis of garbage is subjected to multiple heat exchange with dechlorination reaction gas, catalytic combustion gas and air through a heat exchanger, waste heat in different waste gases can be fully utilized, the air is heated to a certain temperature and then enters a garbage combustion chamber to carry out pyrolysis treatment on the garbage, and the purposes of environmental protection and energy saving are achieved;

2. an active carbon adsorption tower, a dry desulfurization reactor and a dry dechlorination reactor are arranged behind the electric collection and dust removal composite tar removal device, and the active carbon adsorption tower can further remove residual substances such as tar, dioxin and the like in the garbage pyrolysis flue gas; the dry desulfurization reactor is provided with a high-efficiency desulfurizer prepared from calcium oxide, an auxiliary agent, silica sol and water, and can be used for treating SO in flue gas₂Dry removal is carried out, so that acid and alkali waste liquid is prevented from being generated to cause secondary pollution; carbon-doped gamma-Al modified by alkaline earth metal in dry dechlorination reactor₂O₃The composite material has larger specific surface area and pore volume, stronger adsorption capacity and stronger selectivity, can efficiently and selectively adsorb HF and HCl in the flue gas, and has large adsorption capacity;

3. the catalytic combustor adopts Ti-MCM-41 or TS-1 molecular sieve as a carrier, Pt and PtS₂As active component, MnO₂、Co₂O₃、CeO₂The catalyst prepared by one or more auxiliary agents has good sulfur resistance and chlorine resistance, the activation temperature is low, the catalytic combustion can be stably carried out at 120-200 ℃, the conversion rate of CO can reach 94% after the catalytic combustion at 150 ℃, and the excessive emission of carbon monoxide can be effectively prevented;

4. after the outlet gas of the catalytic combustor is treated by the heat exchanger, the temperature of the gas can be effectively reduced, and pollutants such as particulate matters, smoke dust, dioxin, tar and SO in the waste combustion flue gas can be effectively removed by the invention₂HCl and other irritant gases, and the like, and the treated tail gas can reach the standard emission, and meets the pollution control standard of domestic waste incineration (GB 18485-2014).

Drawings

FIG. 1 is a schematic diagram of the system of the present invention;

in the figure: 1: garbage combustion chamber, 1-1: garbage combustion flue gas outlet, 1-2: tube wall outlet, 1-3: tube wall inlet, 1-4: garbage combustion chamber air inlet, 1-5 garbage flue gas collector mouth, 2: heat exchanger I, 2-1: high-temperature gas inlet of heat exchanger I, 2-2: high-temperature gas outlet of heat exchanger I, 2-3: low-temperature gas inlet of heat exchanger I, 2-4: i low-temperature gas outlet of heat exchanger, 3: cyclone dust collector, 3-1: cyclone gas inlet, 3-2: cyclone gas outlet, 4: electric collection dust removal composite tar removal device, 4-1: device gas inlet, 4-2: device gas outlet, 5: activated carbon adsorption tower, 5-1: gas inlet of adsorption tower, 5-2: gas outlet of adsorption tower, 6: dry desulfurization reactor, 6-1: gas inlet of dry desulfurization reactor, 6-2: gas outlet of dry desulfurization reactor, 7: a dry dechlorination reactor, 7-1: gas inlet of a dry dechlorination reactor, 7-2: gas outlet of the dry dechlorination reactor, 8: catalytic combustor, 8-1: catalytic burner gas inlet, 8-2: catalytic burner gas outlet, 8-3 catalytic burner air inlet, 9: chimney, 9-1: chimney inlet, 10: heat exchanger II, 10-1: a low-temperature gas inlet of a heat exchanger II, 10-2: a low-temperature gas outlet of the heat exchanger II is 10-3: a high-temperature gas inlet of a heat exchanger II, 10-4: high-temperature gas outlet of heat exchanger II, 11: heat exchanger iii, 11-1: high-temperature gas inlet of heat exchanger III, 11-2: a high-temperature gas outlet of the heat exchanger III, 11-3: heat exchanger iii low temperature gas inlet, 11-4: and a low-temperature gas outlet of the heat exchanger III.

Detailed Description

The invention is further described with reference to the accompanying drawings, but the invention is not limited in any way, and any alterations or substitutions based on the teaching of the invention are within the scope of the invention.

As shown in the attached figure 1, the invention comprises a garbage combustion chamber 1, a heat exchanger I2, a cyclone dust collector 3, an electric collection dust removal composite tar removal device 4, an active carbon adsorption tower 5, a dry desulfurization reactor 6, a dry dechlorination reactor 7, a catalytic burner 8, a chimney 9, a heat exchanger II 10 and a heat exchanger III 11, wherein a garbage combustion flue gas outlet 1-1 of the garbage combustion chamber 1 is connected with a high-temperature gas inlet 2-1 of the heat exchanger I through a pipeline, a high-temperature gas outlet 2-2 of the heat exchanger I is connected with a cyclone dust collector gas inlet 3-1 of the cyclone dust collector 3 through a pipeline, a cyclone dust collector gas outlet 3-2 is connected with a device gas inlet 4-1 of the electric collection dust removal composite tar removal device 4 through a pipeline, a device gas outlet 4-2 is connected with an adsorption tower gas inlet 5-1 of the carbon adsorption tower 5 through a pipeline, the gas outlet 5-2 of the adsorption tower is connected with the gas inlet 6-1 of the dry desulphurization reactor 6 by a pipeline, the gas outlet 6-2 of the dry desulphurization reactor is connected with the gas inlet 7-1 of the dry dechlorination reactor 7 by a pipeline, the gas outlet 7-2 of the dry dechlorination reactor is connected with the low-temperature gas inlet 2-3 of the heat exchanger I by a pipeline, the upper end of the pipe wall of the garbage combustion chamber 1 is provided with a pipe wall outlet 1-2, the lower end of the pipe wall is provided with a pipe wall inlet 1-3, the low-temperature gas outlet 2-4 of the heat exchanger I is connected with the pipe wall inlet 1-3 by a pipeline, the pipe wall outlet 1-2 is connected with the low-temperature gas inlet 10-1 of the heat exchanger II by a pipeline, the low-temperature gas outlet 10-2 of the heat exchanger II is connected with the gas inlet 8-1 of the catalytic combustor 8 by a pipeline, the gas outlet 8-2 of the catalytic combustor is connected with the high-temperature gas inlet 10-3 of the heat exchanger II through a pipeline, the high-temperature gas outlet 10-4 of the heat exchanger II is connected with the high-temperature gas inlet 11-1 of the heat exchanger III 11 through a pipeline, the high-temperature gas outlet 11-2 of the heat exchanger III is connected with the chimney inlet 9-1 of the chimney 9 through a pipeline, the low-temperature gas inlet 11-3 of the heat exchanger III is an air inlet, and the low-temperature gas outlet 11-4 of the heat exchanger III is respectively connected with the air inlet 1-4 of the garbage combustion chamber 1 of the garbage combustion chamber and the air inlet 8-3 of the catalytic combustor 8 through pipelines.

The garbage combustion chamber 1 comprises a garbage chamber and a combustion chamber, the temperature in the combustion chamber is 700 ℃, high-temperature flue gas generated by garbage pyrolysis is collected by a collector and then discharged from a garbage combustion flue gas outlet 1-1, the temperature of the outlet flue gas is 170-190 ℃, the flow of the flue gas is 1000-10000 m³/h。

The outlet flue gas temperature of the high-temperature gas outlet 2-2 of the heat exchanger I is 120-130 ℃.

The temperature of the outlet gas of the pipe wall outlet 1-2 is 140-160 ℃, and the temperature of the outlet gas of the low-temperature gas outlet 10-2 of the heat exchanger II is 170-190 ℃; the outlet gas temperature of a high-temperature gas outlet 10-4 of the heat exchanger II is 170-190 ℃; the outlet gas temperature of the high-temperature gas outlet 11-2 of the heat exchanger III is 140-150 ℃.

The cyclone dust collector 3 primarily removes large particulate matters, fly ash and other substances in the flue gas.

The electric collection and dust removal composite tar removal device 4 can be an electrostatic dust collector, and fine particulate matters and tar substances in the waste combustion waste gas are removed through the electrostatic dust collector.

The activated carbon adsorption tower 5 adopts activated carbon as an adsorbent to further remove a small amount of residual tar and dioxin substances in the waste combustion waste gas.

The desulfurizer adopted by the dry desulfurization reactor 6 is obtained by mixing and drying calcium oxide, an auxiliary agent, silica sol and water, and specifically comprises the steps of grinding and mixing the calcium oxide, the auxiliary agent and the silica sol in a container, dropwise adding 30mL of water to bond each component at the dropping rate of 1-2 drops/min, continuously rolling and grinding for 60min to make each component uniform, forming, and drying the obtained mixture at 80 ℃ for 12h to obtain the desulfurizer; the mass ratio of the calcium oxide to the auxiliary agent is 32-94: 5-62, and the silica sol accounts for 3-20% of the mass sum of the calcium oxide and the auxiliary agent; the auxiliary agent comprises one or more of ferric oxide, manganese oxide, magnesium oxide, calcium carbonate, cement and carbon slag; desulfurizing agent for removing SO in waste gas₂A major sulfide-containing component; when the auxiliary agent is preferably a mixture of iron oxide, manganese oxide, magnesium oxide, calcium carbonate, cement and carbon slag, the mass ratio of the iron oxide, the manganese oxide, the magnesium oxide, the calcium carbonate, the cement and the carbon slag in the mixture is preferably 1-10: 1-4: 1-8: 5-20: 1-8: 1-12.

The dechlorinating agent adopted by the dry dechlorinating reactor 7 is alkaline earth metal modified carbon-doped gamma-Al₂O₃The composite material is prepared by adopting an isometric immersion method or a sol-gel method. The specific preparation process of the dechlorinating agent can be that a template agent and a carbon source are dissolved in absolute ethyl alcohol to obtain a mixed solution, the concentration of the template agent in the mixed solution is 0.5-1.5 g/L, the concentration of the carbon source is 0.5-2 g/L, 60-70 wt% of nitric acid is added into the mixed solution according to the proportion of 1-2 mL/L, aluminum nitrate is added according to the proportion of 1-1.5 g/L in vigorous stirring, nitrate is added according to the proportion of 0.2-0.8 g/L, and the nitrate is magnesium nitrate and/or calcium nitrate; sealing, stirring at room temperature for 4-6 hours, drying the mixture, and adding N₂Roasting for 4-6 h at 500-600 ℃ in the atmosphere, tabletting, and sieving to obtain 40-60-mesh granules, namely the dechlorinating agent; dechlorinating agent for chlorine-containing components such as HCl, HF and the like in waste pyrolysis waste gasDeep purification is carried out; the outlet gas temperature of a gas outlet 7-2 of the dry dechlorination reactor is 50-70 ℃; the outlet gas temperature of the low-temperature gas outlet 2-4 of the heat exchanger I is 100-120 ℃.

The catalytic combustor 8 contains a sulfur-resistant and chlorine-resistant catalyst material and can catalyze and oxidize CO in the exhaust gas to CO₂Further effectively reducing the concentration of CO in the discharged flue gas, wherein the temperature of the outlet gas of the catalytic combustor gas outlet 8-2 is 200-250 ℃.

The sulfur-resistant and chlorine-resistant catalyst material is prepared from the following components in percentage by weight: 93-97% of carrier, 0.01-0.5% of active component and the balance of cocatalyst, wherein the carrier is Ti-MCM-41 or TS-1 molecular sieve, and the active component is Pt and PtS₂The cocatalyst is MnO₂、Co₂O₃、CeO₂One or more of them at random.

The preparation method comprises the following steps of preparing a Ti-MCM-41 or TS-1 molecular sieve as a carrier by a hydrothermal method, loading an active component on the carrier by an impregnation method, drying, calcining and tabletting to 40-60 meshes to obtain a catalyst, specifically dissolving a platinum salt and a nitrate of a promoter metal in water to obtain an impregnation solution, adding a mesoporous carrier into the impregnation solution, drying and roasting under the stirring condition; wherein the nitrate of the promoter metal is manganese nitrate, the mass ratio of platinum salt to nitrate is 0.043-0.048: 1, the concentration of platinum salt in impregnation liquid is 0.03-0.3 mol/L, the drying temperature is 60 ℃, the drying time is 4h, then the drying is carried out for 1h at the temperature of 70 ℃, the roasting temperature is 550 ℃, the roasting time is 5h, the sulfur-resistant and chlorine-resistant catalyst is prepared, and the catalyst is filled in a catalytic combustor

In percentage by weight, the Ti-MCM-41 molecular sieve contains 2-10% of Ti and 90-98% of Si.

The heat exchanger I2, the heat exchanger II 10 and the heat exchanger III 11 are all tube type heat exchangers, two ends of one heat exchange tube are respectively connected with the high-temperature gas inlet and the high-temperature gas outlet, two ends of the other heat exchange tube are respectively connected with the low-temperature gas inlet and the low-temperature gas outlet, and heat exchange is carried out between gases in the two heat exchange tubes.

The process of the waste pyrolysis and waste gas purification system comprises the steps that combustion flue gas in a waste combustion chamber 1 enters a heat exchanger I2 for heat exchange and cooling, and then the flue gas is sequentially treated by a cyclone dust collector 3, an electric collection and dust removal composite tar removal device 4, an activated carbon adsorption tower 5, a dry desulfurization reactor 6 and a dry dechlorination reactor 7 to obtain low-temperature primary purified gas;

the primary purified gas is subjected to heat exchange and temperature rise respectively through a heat exchanger I2, a garbage combustion chamber 1 and a heat exchanger II 10, and then enters a catalytic combustor 8 for treatment to obtain high-temperature purified gas;

high-temperature purified gas is sent to a heat exchanger II 10 for heat exchange and temperature reduction, and then is subjected to heat exchange and temperature reduction by a heat exchanger III 11, so that the air is subjected to heat exchange and temperature rise; the purified gas after being cooled is discharged out through a chimney 9; the air after temperature rise is sent to the garbage combustion chamber 1 and the catalytic combustor 8 as combustion air.

The working principle and the working process of the system of the invention are as follows: flue gas generated by burning garbage in the garbage burning chamber 1 passes through a garbage flue gas collector port 1-5, a garbage burning flue gas outlet 1-1 and a high-temperature gas inlet 2-1 of a heat exchanger I and enters a heat exchanger I2; then the flue gas is discharged from a high-temperature gas outlet 2-2 of the heat exchanger I to a cyclone dust collector 3 to primarily remove large particulate matters, fly ash and other substances in the flue gas; the flue gas after dust removal is discharged to an electric collection and dust removal composite tar removal device 4 to remove fine particulate matters and tar substances; then removing residual tar and dioxin from the flue gas through an activated carbon adsorption tower 5, purifying sulfide components through a dry desulfurization reactor 6, and purifying chloride components through a dry dechlorination reactor 7 to obtain primary purified gas, wherein the gas temperature is 50-70 ℃; the primary purified gas enters the heat exchanger I from the low-temperature gas inlet of the heat exchanger I for heat exchange and temperature rise, after the temperature rise, the primary purified gas enters the combustion chamber from the low-temperature gas outlet 2-4 and the pipe wall inlet 1-3 of the heat exchanger I for heat exchange and temperature rise, and then enters the heat exchanger II for continuous heat exchange and temperature rise from the pipe wall outlet 1-2 and the low-temperature gas inlet 10-1 of the heat exchanger II; after the temperature is raised, the gas enters a catalytic combustor 8 from a low-temperature gas outlet 10-2 of the heat exchanger II and a gas inlet 8-1 of the catalytic combustor for treatment, so that the concentration of CO in the gas is reduced; and (3) discharging high-temperature purified gas from a gas outlet 8-2 of the catalytic combustor, enabling the high-temperature purified gas to enter a heat exchanger II 10 from a high-temperature gas inlet 10-3 of the heat exchanger II for heat exchange and cooling, enabling the cooled purified gas to enter a heat exchanger III 11 from a high-temperature gas outlet 10-4 of the heat exchanger II and a high-temperature gas inlet 11-1 of the heat exchanger III for heat exchange and cooling again to heat combustion air, enabling the cooled purified gas to be sent to a chimney 9 and discharged outside, and enabling the heated air to be sent to a garbage combustion chamber 1 and the catalytic combustor 8 from a low-temperature gas outlet 11-4 of the heat exchanger III.

The present invention will be further described with reference to examples 1 to 9.

Example 1

The temperature in the combustion chamber of the garbage combustion chamber 1 is 700 ℃, the temperature of the outlet flue gas is 180 ℃, and the flow rate of the flue gas is 1000m³The flue gas enters a heat exchanger I for heat exchange and temperature reduction, and the temperature is reduced to 122 ℃; then the flue gas is sequentially treated by a cyclone dust collector 3, an electric collection and dust removal composite tar removal device 4, an activated carbon adsorption tower 5, a dry desulfurization reactor 6 and a dry dechlorination reactor 7 to obtain low-temperature primary purified gas, wherein the gas temperature is 60 ℃;

wherein, the desulfurizer adopted by the dry desulfurization reactor 6 is prepared by mixing 27.5g of calcium oxide, 5g of ferric oxide, 7.5g of calcium carbonate, 5g of carbon slag, 2.5g of cement and 8.3g of silica sol (wherein SiO is₂30wt.%) in a polyethylene beaker, then dropwise adding 30mL of deionized water to bond the components, wherein the dropping rate is 1-2 drops/min, continuously rolling and grinding for 60min to make the components uniform, then molding, drying the obtained mixture at 80 ℃ for 12h to obtain a desulfurizer, and filling the desulfurizer into a dry desulfurization reactor 6; the dechlorinating agent adopted by the dry dechlorinating reactor 7 is alkaline earth metal modified carbon-doped gamma-Al₂O₃The composite material is prepared by dissolving a template agent and a carbon source in absolute ethyl alcohol to obtain a mixed solution, wherein the concentration of the template agent in the mixed solution is 0.5g/L, the concentration of the carbon source in the mixed solution is 0.5g/L, 60 wt% nitric acid is added into the mixed solution according to the proportion of 1mL/L, aluminum nitrate is added according to the proportion of 1g/L in vigorous stirring, nitrate is added according to the proportion of 0.2g/L, and the nitrate is calcium nitrate; after sealing and stirring at room temperature for 4 hours, the mixture is dried and then stirred under N₂Roasting at 500 deg.C for 4h in atmosphere, tabletting, sieving to obtain 40 mesh granules as dechlorinating agent, and filling the dechlorinating agent into a dry dechlorinating reactor 7;

the temperature of the primary purified gas is raised to 118 ℃ through heat exchange of a heat exchanger I2, the temperature of the primary purified gas is raised to 150 ℃ through heat exchange of a garbage combustion chamber 1, the temperature of the primary purified gas is raised to 180 ℃ through heat exchange of a heat exchanger II 10, and then the primary purified gas enters a catalytic combustor 8 for processing, wherein the flow rate of flue gas is 1000m for carrying out high-temperature plantation/h, and the temperature of the high-temperature purified gas is 225 ℃;

wherein, the anti-sulfur and anti-chlorine catalyst material in the catalytic combustor 8 is prepared by the following components by weight percentage: 94.7 percent of carrier, 0.3 percent of active component and the balance of cocatalyst, wherein the carrier is Ti-MCM-41, and the active component is Pt and PtS₂The cocatalyst is MnO₂The preparation method comprises the following steps of dissolving a platinum salt and a nitrate of a promoter metal in water to obtain an impregnation solution, adding a mesoporous carrier into the impregnation solution, and drying and roasting under stirring conditions, wherein the Ti content and the Si content in the Ti-MCM-41 molecular sieve are respectively 5% and 95%; wherein the nitrate of the promoter metal is manganese nitrate, the mass ratio of the platinum salt to the nitrate is 0.0476:1, the concentration of the platinum salt in the impregnation liquid is 0.03mol/L, the drying temperature is 60 ℃, the drying time is 4h, then the drying is carried out for 1h at the temperature of 70 ℃, the roasting temperature is 550 ℃, the roasting time is 5h, the sulfur-resistant and chlorine-resistant catalyst is prepared, and the catalyst is filled in a catalytic combustor;

high-temperature purified gas is sent to a heat exchanger II for heat exchange and temperature reduction to 180 ℃, and then is subjected to heat exchange and temperature reduction to 140 ℃ in a heat exchanger III 11, so that air is subjected to heat exchange and temperature rise; the purified gas after being cooled is discharged out through a chimney 9; the air after temperature rise is sent to the garbage combustion chamber 1 and the catalytic combustor 8 as combustion air.

Example 2

The temperature in the combustion chamber of the garbage combustion chamber 1 is 700 ℃, the temperature of the outlet flue gas is 183 ℃, and the flow rate of the flue gas is 1500m³The flue gas enters a heat exchanger I for heat exchange and temperature reduction, and the temperature is reduced to 128 ℃; then the flue gas is sequentially treated by a cyclone dust collector 3, an electric collection and dust removal composite tar removal device 4, an activated carbon adsorption tower 5, a dry desulphurization reactor 6 and a dry dechlorination reactor 7 to obtain low-temperature primary purified gas, wherein the gas temperature is 62 ℃;

wherein, the desulfurizer adopted by the dry desulfurization reactor 6 is prepared by mixing 27.5g of calcium oxide, 5g of ferric oxide, 7.5g of calcium carbonate, 5g of carbon slag, 2.5g of cement and 8.3g of silica sol (wherein SiO is₂In an amount of 30wt.%) in a polyethylene beakerGrinding and mixing, dropwise adding 30mL of deionized water to bond the components at the dropping rate of 1-2 drops/min, continuously rolling and grinding for 60min to make the components uniform, molding, drying the obtained mixture at 80 ℃ for 12h to obtain a desulfurizer, and filling the desulfurizer into a dry desulfurization reactor 6; the dechlorinating agent adopted by the dry dechlorinating reactor 7 is alkaline earth metal modified carbon-doped gamma-Al₂O₃The composite material is prepared by dissolving a template agent and a carbon source in absolute ethyl alcohol to obtain a mixed solution, wherein the concentration of the template agent in the mixed solution is 1.5g/L, the concentration of the carbon source in the mixed solution is 2g/L, 70wt% nitric acid is added into the mixed solution according to the proportion of 2mL/L, aluminum nitrate is added according to the proportion of 1.5g/L in vigorous stirring, nitrate is added according to the proportion of 0.8g/L, and the nitrate is magnesium nitrate; after sealing and stirring at room temperature for 6 hours, the mixture is dried and then stirred under N₂Roasting at 600 ℃ for 6 hours in the atmosphere, tabletting and sieving to obtain 60-mesh granules, namely dechlorinating agent, and filling the dechlorinating agent into a dry dechlorinating reactor 7;

the temperature of the primary purified gas is increased to 117 ℃ through heat exchange of a heat exchanger I2, the temperature is increased to 153 ℃ through heat exchange of a garbage combustion chamber 1, the temperature is increased to 183 ℃ through heat exchange of a heat exchanger II 10, then the primary purified gas enters a catalytic combustor 8 for processing, the flow rate of flue gas is 1500m for carrying out heavy planting/h, and high-temperature purified gas is obtained, wherein the temperature is 213 ℃;

wherein, the anti-sulfur and anti-chlorine catalyst material in the catalytic combustor 8 is prepared by the following components by weight percentage: 94.7 percent of carrier, 0.3 percent of active component and the balance of cocatalyst, wherein the carrier is Ti-MCM-41, and the active component is Pt and PtS₂The cocatalyst is MnO₂The preparation method comprises the following steps of dissolving a platinum salt and a nitrate of a promoter metal in water to obtain an impregnation solution, adding a mesoporous carrier into the impregnation solution, and drying and roasting under stirring conditions, wherein the Ti content and the Si content in the Ti-MCM-41 molecular sieve are respectively 5% and 95%; wherein the nitrate of the promoter metal is manganese nitrate, the mass ratio of the platinum salt to the nitrate is 0.0476:1, the concentration of the platinum salt in the impregnation liquid is 0.03mol/L, the drying temperature is 60 ℃, the drying time is 4h, then the drying is carried out for 1h at the temperature of 70 ℃, the roasting temperature is 550 ℃, the roasting time is 5h, the sulfur-resistant and chlorine-resistant catalyst is prepared, and the catalyst is prepared by the steps ofThe catalyst is filled in the catalytic combustor;

sending the high-temperature purified gas to a heat exchanger II for heat exchange and cooling to 183 ℃, then carrying out heat exchange and cooling to 142 ℃ in a heat exchanger III 11, and carrying out heat exchange and heating on air; the purified gas after being cooled is discharged out through a chimney 9; the air after temperature rise is sent to the garbage combustion chamber 1 and the catalytic combustor 8 as combustion air.

Example 3

The temperature in the combustion chamber of the garbage combustion chamber 1 is 700 ℃, the temperature of the outlet flue gas is 185 ℃, and the flow rate of the flue gas is 2000m³The flue gas enters a heat exchanger I for heat exchange and temperature reduction, and the temperature is reduced to 130 ℃; then the flue gas is sequentially treated by a cyclone dust collector 3, an electric collection and dust removal composite tar removal device 4, an activated carbon adsorption tower 5, a dry desulfurization reactor 6 and a dry dechlorination reactor 7 to obtain low-temperature primary purified gas, wherein the gas temperature is 65 ℃;

wherein, the desulfurizer adopted by the dry desulfurization reactor 6 is prepared by mixing 28.5g of calcium oxide, 2.5g of magnesium oxide, 5g of ferric oxide, 1.5g of manganese oxide, 7.5g of calcium carbonate, 2.5g of cement and 8.3g of silica sol (wherein SiO is₂30wt.%) in a polyethylene beaker, then dropwise adding 30mL of deionized water to bond the components, wherein the dropping rate is 1-2 drops/min, continuously rolling and grinding for 60min to make the components uniform, then molding, drying the obtained mixture at 80 ℃ for 12h to obtain a desulfurizer, and filling the desulfurizer into a dry desulfurization reactor 6; the dechlorinating agent adopted by the dry dechlorinating reactor 7 is alkaline earth metal modified carbon-doped gamma-Al₂O₃The composite material is prepared by dissolving a template agent and a carbon source in absolute ethyl alcohol to obtain a mixed solution, wherein the concentration of the template agent in the mixed solution is 1.0g/L, the concentration of the carbon source in the mixed solution is 1.25g/L, 65 wt% nitric acid is added into the mixed solution according to the proportion of 1.5mL/L, aluminum nitrate is added according to the proportion of 1.25g/L in vigorous stirring, nitrate is added according to the proportion of 0.5g/L, and the nitrate is magnesium nitrate and calcium nitrate; after sealing and stirring at room temperature for 5 hours, the mixture is dried and then stirred under N₂Roasting at 550 ℃ for 5 hours in the atmosphere, tabletting and sieving to obtain 50-mesh granules, namely dechlorinating agent, and filling the dechlorinating agent into a dry dechlorinating reactor 7;

the temperature of the primary purified gas is raised to 120 ℃ through heat exchange of a heat exchanger I2, raised to 155 ℃ through heat exchange of a garbage combustion chamber 1, raised to 185 ℃ through heat exchange of a heat exchanger II 10, and then enters a catalytic combustor 8 for processing, the flow rate of flue gas is 2000m for carrying out high-temperature plantation/h, and the high-temperature purified gas is obtained, and the temperature is 215 ℃;

wherein, the anti-sulfur and anti-chlorine catalyst material in the catalytic combustor 8 is prepared by the following components by weight percentage: 94.7 percent of carrier, 0.3 percent of active component and the balance of cocatalyst, wherein the carrier is Ti-MCM-41, and the active component is Pt and PtS₂The cocatalyst is MnO₂The preparation method comprises the following steps of dissolving a platinum salt and a nitrate of a promoter metal in water to obtain an impregnation solution, adding a mesoporous carrier into the impregnation solution, and drying and roasting under stirring conditions, wherein the Ti content and the Si content in the Ti-MCM-41 molecular sieve are respectively 5% and 95%; wherein the nitrate of the promoter metal is manganese nitrate and cobalt nitrate, the mass ratio of platinum salt to nitrate is 0.043:1, the concentration of platinum salt in the impregnation liquid is 0.3mol/L, the drying temperature is 60 ℃, the drying time is 4h, then the drying is carried out for 1h at the temperature of 70 ℃, the roasting temperature is 550 ℃, the roasting time is 5h, the sulfur-resistant and chlorine-resistant catalyst is prepared, and the catalyst is filled in a catalytic combustor;

sending the high-temperature purified gas to a heat exchanger II for heat exchange and cooling to 185 ℃, then carrying out heat exchange and cooling to 145 ℃ in a heat exchanger III 11, and carrying out heat exchange and heating on air; the purified gas after being cooled is discharged out through a chimney 9; the air after temperature rise is sent to the garbage combustion chamber 1 and the catalytic combustor 8 as combustion air.

Example 4

The temperature in the combustion chamber of the garbage combustion chamber 1 is 700 ℃, the temperature of the outlet flue gas is 185 ℃, and the flow rate of the flue gas is 5500m³The flue gas enters a heat exchanger I for heat exchange and temperature reduction, and the temperature is reduced to 130 ℃; then the flue gas is sequentially treated by a cyclone dust collector 3, an electric collection and dust removal composite tar removal device 4, an activated carbon adsorption tower 5, a dry desulfurization reactor 6 and a dry dechlorination reactor 7 to obtain low-temperature primary purified gas, wherein the gas temperature is 65 ℃;

wherein, the desulfurizer adopted by the dry desulfurization reactor 6 is calcium oxide, magnesium oxide, ferric oxide, manganese oxide, magnesium oxide, calcium carbonate, cement, carbon slag and silica sol (wherein SiO is₂30wt.%) is ground and mixed in a polyethylene beaker, the mass ratio of calcium oxide to an auxiliary agent is 32:5, silica sol accounts for 3% of the mass sum of the calcium oxide and the auxiliary agent, the mass ratio of iron oxide, manganese oxide, magnesium oxide, calcium carbonate, cement and carbon slag is 1:1:1:5:1:12, 30mL of deionized water is dripped dropwise to bond each component, the dripping speed is 1-2 drops/min, the grinding is continued for 60min to make each component uniform, the mixture is molded, the obtained mixture is dried at 80 ℃ for 12h to obtain a desulfurizer, and the desulfurizer is filled in a dry desulfurization reactor 6; the dechlorinating agent adopted by the dry dechlorinating reactor 7 is alkaline earth metal modified carbon-doped gamma-Al₂O₃The composite material is prepared by dissolving a template agent and a carbon source in absolute ethyl alcohol to obtain a mixed solution, wherein the concentration of the template agent in the mixed solution is 0.9g/L, the concentration of the carbon source in the mixed solution is 1.3g/L, 60 wt% nitric acid is added into the mixed solution according to the proportion of 1.5mL/L, aluminum nitrate is added according to the proportion of 1.3g/L in vigorous stirring, nitrate is added according to the proportion of 0.5g/L, and the nitrate is magnesium nitrate and calcium nitrate with the mass ratio of 1: 1; after sealing and stirring at room temperature for 5 hours, the mixture is dried and then stirred under N₂Roasting at 550 ℃ for 5 hours in the atmosphere, tabletting and sieving to obtain 50-mesh granules, namely dechlorinating agent, and filling the dechlorinating agent into a dry dechlorinating reactor 7;

the temperature of the primary purified gas is raised to 120 ℃ through heat exchange of a heat exchanger I2, raised to 155 ℃ through heat exchange of a garbage combustion chamber 1, raised to 185 ℃ through heat exchange of a heat exchanger II 10, and then enters a catalytic combustor 8 for processing, the flow rate of flue gas is 2000m for carrying out high-temperature plantation/h, and the high-temperature purified gas is obtained, and the temperature is 215 ℃;

wherein, the anti-sulfur and anti-chlorine catalyst material in the catalytic combustor 8 is prepared by the following components by weight percentage: 93 percent of carrier, 0.01 percent of active component and the balance of cocatalyst, wherein the carrier is Ti-MCM-41, and the active component is Pt and PtS₂The cocatalyst is MnO₂The Ti-MCM-41 molecular sieve comprises 2 wt% of Ti and 98 wt% of Si, and is prepared by dissolving a platinum salt and a nitrate of a promoter metal in water to obtain an impregnation solution, adding a mesoporous carrier into the impregnation solution, and drying and roasting under stirring; wherein the cocatalystThe nitrate of the metal is manganese nitrate and cobalt nitrate, the mass ratio of the platinum salt to the nitrate is 0.043:1, the concentration of the platinum salt in the impregnation liquid is 0.03mol/L, the drying temperature is 60 ℃, the drying time is 4h, then the drying is carried out for 1h at the temperature of 70 ℃, the roasting temperature is 550 ℃, the roasting time is 5h, the sulfur-resistant and chlorine-resistant catalyst is prepared, and the catalyst is filled in a catalytic combustor;

sending the high-temperature purified gas to a heat exchanger II for heat exchange and cooling to 185 ℃, then carrying out heat exchange and cooling to 145 ℃ in a heat exchanger III 11, and carrying out heat exchange and heating on air; the purified gas after being cooled is discharged out through a chimney 9; the air after temperature rise is sent to the garbage combustion chamber 1 and the catalytic combustor 8 as combustion air.

Example 5

The temperature in the combustion chamber of the garbage combustion chamber 1 is 700 ℃, the temperature of the outlet flue gas is 185 ℃, and the flow rate of the flue gas is 3000m³The flue gas enters a heat exchanger I for heat exchange and temperature reduction, and the temperature is reduced to 130 ℃; then the flue gas is sequentially treated by a cyclone dust collector 3, an electric collection and dust removal composite tar removal device 4, an activated carbon adsorption tower 5, a dry desulfurization reactor 6 and a dry dechlorination reactor 7 to obtain low-temperature primary purified gas, wherein the gas temperature is 65 ℃;

wherein, the desulfurizer adopted by the dry desulfurization reactor 6 is calcium oxide, magnesium oxide, ferric oxide, manganese oxide, magnesium oxide, calcium carbonate, cement, carbon slag and silica sol (wherein SiO is₂30wt.%) is ground and mixed in a polyethylene beaker, the mass ratio of calcium oxide to an auxiliary agent is 94:62, silica sol accounts for 20% of the mass sum of the calcium oxide and the auxiliary agent, the mass ratio of iron oxide, manganese oxide, magnesium oxide, calcium carbonate, cement and carbon slag is 10:4:8:20:8:1, 30mL of deionized water is dripped dropwise to bond the components, the dripping rate is 1-2 drops/min, the grinding is continued for 60min to make the components uniform, the mixture is molded, the obtained mixture is dried at 80 ℃ for 12h to obtain a desulfurizer, and the desulfurizer is filled in a dry desulfurization reactor 6; the dechlorinating agent adopted by the dry dechlorinating reactor 7 is alkaline earth metal modified carbon-doped gamma-Al₂O₃The composite material is prepared by dissolving a template agent and a carbon source in absolute ethyl alcohol to obtain a mixed solution, wherein the concentration of the template agent and the carbon source in the mixed solution is 0.9g/L and 1.3g/L, and the concentration of the carbon source is 1.5mL/LAdding 60 wt% of nitric acid into the mixed solution, adding aluminum nitrate according to the proportion of 1.3g/L in vigorous stirring, and adding nitrate according to the proportion of 0.5g/L, wherein the nitrate is magnesium nitrate and calcium nitrate, and the mass ratio of the magnesium nitrate to the calcium nitrate is 1: 1; after sealing and stirring at room temperature for 5 hours, the mixture is dried and then stirred under N₂Roasting at 550 ℃ for 5 hours in the atmosphere, tabletting and sieving to obtain 50-mesh granules, namely dechlorinating agent, and filling the dechlorinating agent into a dry dechlorinating reactor 7;

the temperature of the primary purified gas is raised to 120 ℃ through heat exchange of a heat exchanger I2, raised to 155 ℃ through heat exchange of a garbage combustion chamber 1, raised to 185 ℃ through heat exchange of a heat exchanger II 10, and then enters a catalytic combustor 8 for processing, the flow rate of flue gas is 2000m for carrying out high-temperature plantation/h, and the high-temperature purified gas is obtained, and the temperature is 215 ℃;

wherein, the anti-sulfur and anti-chlorine catalyst material in the catalytic combustor 8 is prepared by the following components by weight percentage: 97 percent of carrier, 0.5 percent of active component and the balance of cocatalyst, wherein the carrier is Ti-MCM-41, and the active component is Pt and PtS₂The cocatalyst is MnO₂The preparation method comprises the following steps of dissolving a platinum salt and a nitrate of a promoter metal in water to obtain an impregnation solution, adding a mesoporous carrier into the impregnation solution, and drying and roasting under stirring conditions, wherein the Ti content in the Ti-MCM-41 molecular sieve is 10% and the Si content is 90% by weight; wherein the nitrate of the promoter metal is manganese nitrate and cobalt nitrate, the mass ratio of platinum salt to nitrate is 0.048:1, the concentration of platinum salt in the impregnation liquid is 0.3mol/L, the drying temperature is 60 ℃, the drying time is 4h, then the drying is carried out for 1h at the temperature of 70 ℃, the roasting temperature is 550 ℃, the roasting time is 5h, the sulfur-resistant and chlorine-resistant catalyst is prepared, and the catalyst is filled in a catalytic combustor;

sending the high-temperature purified gas to a heat exchanger II for heat exchange and cooling to 185 ℃, then carrying out heat exchange and cooling to 145 ℃ in a heat exchanger III 11, and carrying out heat exchange and heating on air; the purified gas after being cooled is discharged out through a chimney 9; the air after temperature rise is sent to the garbage combustion chamber 1 and the catalytic combustor 8 as combustion air.

Example 6

The temperature in the combustion chamber of the garbage combustion chamber 1 is 700 ℃, the temperature of the outlet flue gas is 185 ℃, and the flow rate of the flue gas is 185 DEG CIs 3000m³The flue gas enters a heat exchanger I for heat exchange and temperature reduction, and the temperature is reduced to 130 ℃; then the flue gas is sequentially treated by a cyclone dust collector 3, an electric collection and dust removal composite tar removal device 4, an activated carbon adsorption tower 5, a dry desulfurization reactor 6 and a dry dechlorination reactor 7 to obtain low-temperature primary purified gas, wherein the gas temperature is 65 ℃;

wherein, the desulfurizer adopted by the dry desulfurization reactor 6 is calcium oxide, magnesium oxide, ferric oxide, manganese oxide, magnesium oxide, calcium carbonate, cement, carbon slag and silica sol (wherein SiO is₂30wt.%) is ground and mixed in a polyethylene beaker, the mass ratio of calcium oxide to auxiliary agent is 50:59, silica sol accounts for 17% of the sum of the mass of calcium oxide and auxiliary agent, the mass ratio of iron oxide, manganese oxide, magnesium oxide, calcium carbonate, cement and carbon slag is 5.5:2.5:4.5:12.5:4.5:6.5, 30mL of deionized water is dripped dropwise to bond the components, the dripping speed is 1-2 drops/min, the grinding is continued for 60min to make the components uniform, the mixture is formed, the mixture is dried at 80 ℃ for 12h to obtain the desulfurizer, and the desulfurizer is filled in a dry desulfurization reactor 6; the dechlorinating agent adopted by the dry dechlorinating reactor 7 is alkaline earth metal modified carbon-doped gamma-Al₂O₃The composite material is prepared by dissolving a template agent and a carbon source in absolute ethyl alcohol to obtain a mixed solution, wherein the concentration of the template agent in the mixed solution is 0.9g/L, the concentration of the carbon source in the mixed solution is 1.3g/L, 60 wt% nitric acid is added into the mixed solution according to the proportion of 1.5mL/L, aluminum nitrate is added according to the proportion of 1.3g/L in vigorous stirring, nitrate is added according to the proportion of 0.5g/L, and the nitrate is magnesium nitrate and calcium nitrate with the mass ratio of 1: 1; after sealing and stirring at room temperature for 5 hours, the mixture is dried and then stirred under N₂Roasting at 550 ℃ for 5 hours in the atmosphere, tabletting and sieving to obtain 50-mesh granules, namely dechlorinating agent, and filling the dechlorinating agent into a dry dechlorinating reactor 7;

the temperature of the primary purified gas is raised to 120 ℃ through heat exchange of a heat exchanger I2, raised to 155 ℃ through heat exchange of a garbage combustion chamber 1, raised to 185 ℃ through heat exchange of a heat exchanger II 10, and then enters a catalytic combustor 8 for processing, the flow rate of flue gas is 2000m for carrying out high-temperature plantation/h, and the high-temperature purified gas is obtained, and the temperature is 215 ℃;

therein, in the catalytic combustor 8The sulfur-resistant and chlorine-resistant catalyst material is prepared from the following components in percentage by weight: 95% of carrier, 0.255% of active component and the balance of cocatalyst, wherein the carrier is Ti-MCM-41, and the active component is Pt and PtS₂The cocatalyst is MnO₂The Ti-MCM-41 molecular sieve comprises 6 wt% of Ti and 94 wt% of Si, and is prepared by dissolving a platinum salt and a nitrate of a promoter metal in water to obtain an impregnation solution, adding a mesoporous carrier into the impregnation solution, and drying and roasting under stirring; wherein the nitrate of the promoter metal is manganese nitrate and cobalt nitrate, the mass ratio of the platinum salt to the nitrate is 0.0455:1, the concentration of the platinum salt in the impregnation liquid is 0.165mol/L, the drying temperature is 60 ℃, the drying time is 4h, then the drying is carried out for 1h at the temperature of 70 ℃, the roasting temperature is 550 ℃, the roasting time is 5h, the sulfur-resistant and chlorine-resistant catalyst is prepared, and the catalyst is filled in a catalytic combustor;

sending the high-temperature purified gas to a heat exchanger II for heat exchange and cooling to 185 ℃, then carrying out heat exchange and cooling to 145 ℃ in a heat exchanger III 11, and carrying out heat exchange and heating on air; the purified gas after being cooled is discharged out through a chimney 9; the air after temperature rise is sent to the garbage combustion chamber 1 and the catalytic combustor 8 as combustion air.

Example 7

The temperature in the combustion chamber of the garbage combustion chamber 1 is 700 ℃, the temperature of the outlet flue gas is 170 ℃, and the flow rate of the flue gas is 1000m³The flue gas enters a heat exchanger I for heat exchange and temperature reduction, and the temperature is reduced to 120 ℃; then the flue gas is sequentially treated by a cyclone dust collector 3, an electric collection and dust removal composite tar removal device 4, an activated carbon adsorption tower 5, a dry desulfurization reactor 6 and a dry dechlorination reactor 7 to obtain low-temperature primary purified gas, wherein the gas temperature is 50 ℃;

the desulfurizer adopted by the dry desulfurization reactor 6 is obtained by mixing and drying calcium oxide, an auxiliary agent, silica sol and water, wherein the mass ratio of the calcium oxide to the auxiliary agent is 32:5, and the silica sol accounts for 3% of the mass sum of the calcium oxide and the auxiliary agent; the auxiliary agent is ferric oxide; the dechlorinating agent adopted by the dry dechlorinating reactor 7 is alkaline earth metal modified carbon-doped gamma-Al₂O₃The composite material is prepared by adopting an isometric impregnation method;

the temperature of the primary purified gas is raised to 100 ℃ through heat exchange of a heat exchanger I2, the temperature of the primary purified gas is raised to 140 ℃ through heat exchange of a garbage combustion chamber 1, the temperature of the primary purified gas is raised to 170 ℃ through heat exchange of a heat exchanger II 10, and then the primary purified gas enters a catalytic combustor 8 for processing, wherein the flow rate of flue gas is 1000m for carrying out high-temperature plantation/h, and the temperature of the high-temperature purified gas is 200 ℃;

wherein, the anti-sulfur and anti-chlorine catalyst material in the catalytic combustor 8 is prepared by the following components by weight percentage: 93 percent of carrier, 0.01 percent of active component and the balance of cocatalyst, wherein the carrier is Ti-MCM-41, and the active component is Pt and PtS₂The cocatalyst is Co₂O₃；

Sending the high-temperature purified gas to a heat exchanger II for heat exchange and cooling to 170 ℃, then carrying out heat exchange and cooling to 140 ℃ in a heat exchanger III 11, and carrying out heat exchange and heating on air; the purified gas after being cooled is discharged out through a chimney 9; the air after temperature rise is sent to the garbage combustion chamber 1 and the catalytic combustor 8 as combustion air.

Example 8

The temperature in the combustion chamber of the garbage combustion chamber 1 is 700 ℃, the temperature of the outlet flue gas is 190 ℃, and the flow rate of the flue gas is 10000m³The flue gas enters a heat exchanger I for heat exchange and temperature reduction, and the temperature is reduced to 130 ℃; then the flue gas is sequentially treated by a cyclone dust collector 3, an electric collection and dust removal composite tar removal device 4, an activated carbon adsorption tower 5, a dry desulfurization reactor 6 and a dry dechlorination reactor 7 to obtain low-temperature primary purified gas, wherein the gas temperature is 70 ℃;

the desulfurizer adopted by the dry desulfurization reactor 6 is obtained by mixing and drying calcium oxide, an auxiliary agent, silica sol and water, wherein the mass ratio of the calcium oxide to the auxiliary agent is 94:62, and the silica sol accounts for 20% of the mass sum of the calcium oxide and the auxiliary agent; the auxiliary agent is manganese oxide; the dechlorinating agent adopted by the dry dechlorinating reactor 7 is alkaline earth metal modified carbon-doped gamma-Al₂O₃The composite material is prepared by adopting a sol-gel method;

the temperature of the primary purified gas is raised to 120 ℃ through heat exchange of a heat exchanger I2, the temperature of the primary purified gas is raised to 160 ℃ through heat exchange of a garbage combustion chamber 1, the temperature of the primary purified gas is raised to 190 ℃ through heat exchange of a heat exchanger II 10, and then the primary purified gas enters a catalytic combustor 8 for processing, wherein the flow rate of flue gas is 1000m for carrying out high-temperature plantation/h, and the temperature of the high-temperature purified gas is 250 ℃;

in which catalytic combustion is carried outThe sulfur-resistant and chlorine-resistant catalyst material in the reactor 8 is prepared from the following components in percentage by weight: 97 percent of carrier, 0.5 percent of active component and the balance of cocatalyst, wherein the carrier is Ti-MCM-41, and the active component is Pt and PtS₂The cocatalyst is CeO₂；

High-temperature purified gas is sent to a heat exchanger II for heat exchange and temperature reduction to 190 ℃, and then is subjected to heat exchange and temperature reduction to 150 ℃ in a heat exchanger III 11, so that air is subjected to heat exchange and temperature rise; the purified gas after being cooled is discharged out through a chimney 9; the air after temperature rise is sent to the garbage combustion chamber 1 and the catalytic combustor 8 as combustion air.

Example 9

The temperature in the combustion chamber of the garbage combustion chamber 1 is 700 ℃, the temperature of the outlet flue gas is 180 ℃, and the flow rate of the flue gas is 3000m³The flue gas enters a heat exchanger I for heat exchange and temperature reduction, and the temperature is reduced to 125 ℃; then the flue gas is sequentially treated by a cyclone dust collector 3, an electric collection and dust removal composite tar removal device 4, an activated carbon adsorption tower 5, a dry desulfurization reactor 6 and a dry dechlorination reactor 7 to obtain low-temperature primary purified gas, wherein the gas temperature is 60 ℃;

the desulfurizer adopted by the dry desulfurization reactor 6 is obtained by mixing and drying calcium oxide, an auxiliary agent, silica sol and water, wherein the mass ratio of the calcium oxide to the auxiliary agent is 63:33.5, and the silica sol accounts for 11.5% of the mass sum of the calcium oxide and the auxiliary agent; the auxiliary agent is magnesium oxide; the dechlorinating agent adopted by the dry dechlorinating reactor 7 is alkaline earth metal modified carbon-doped gamma-Al₂O₃The composite material adopts an isometric impregnation method;

the temperature of the primary purified gas is raised to 110 ℃ through heat exchange of a heat exchanger I2, the temperature of the primary purified gas is raised to 150 ℃ through heat exchange of a garbage combustion chamber 1, the temperature of the primary purified gas is raised to 180 ℃ through heat exchange of a heat exchanger II 10, and then the primary purified gas enters a catalytic combustor 8 for processing, wherein the flow rate of flue gas is 1000m for carrying out high-temperature plantation/h, and the temperature of the high-temperature purified gas is 225 ℃;

wherein, the anti-sulfur and anti-chlorine catalyst material in the catalytic combustor 8 is prepared by the following components by weight percentage: 95% of carrier, 0.255% of active component and the balance of cocatalyst, wherein the carrier is TS-1 molecular sieve, and the active component is Pt and PtS₂The cocatalyst is MnO₂、Co₂O₃、CeO₂；

High-temperature purified gas is sent to a heat exchanger II for heat exchange and temperature reduction to 180 ℃, and then is subjected to heat exchange and temperature reduction to 145 ℃ in a heat exchanger III 11, so that air is subjected to heat exchange and temperature rise; the purified gas after being cooled is discharged out through a chimney 9; the air after temperature rise is sent to the garbage combustion chamber 1 and the catalytic combustor 8 as combustion air.