CN217251456U

CN217251456U - In-situ oxidation hazardous waste disposal system

Info

Publication number: CN217251456U
Application number: CN202220532279.8U
Authority: CN
Inventors: 符国华; 符蓉
Original assignee: Jiangsu Carbon Peak Blue Energy Saving Technology Co ltd
Current assignee: Jiangsu Blue Green Environmental Protection Technology Co ltd
Priority date: 2022-03-11
Filing date: 2022-03-11
Publication date: 2022-08-23
Anticipated expiration: 2032-03-11

Abstract

The utility model provides a useless processing system of normal position oxidation danger, it includes: a pretreatment mixing granulation system, a belt type in-situ oxidation device, a flue gas circulation system and a tail gas treatment system; the pretreatment mixing granulation system is connected with the belt type in-situ oxidation device; the material vehicle of the belt type in-situ oxidation device sequentially passes through a drying section, a preheating section, an oxidation section and a cooling section of the flue gas circulating system; the flue gas circulation system is connected with the tail gas treatment system. The utility model discloses a belt normal position oxidation method gets rid of the organic matter in the useless salt, has realized getting rid of the organic matter in the danger is useless to reach the danger and abolish "danger" of solving, become "useless" purpose for "precious", realized circular economy's effect.

Description

In-situ oxidation hazardous waste disposal system

Technical Field

The utility model belongs to the technical field of solid waste and hazardous waste handles technique and specifically relates to a useless processing system of normal position oxidation danger is related to.

Background

The chemical industry generates a large amount of industrial waste salt of toxic and harmful substances every year, wherein the industrial waste salt comprises sodium sulfate, sodium chloride, phosphate, nitrate and the like, and how to remove organic matters in the waste salt is always a technical bottleneck restricting the waste salt generation industry. The industrial waste salt containing high organic matters is used as dangerous waste, only a small amount of the industrial waste salt is treated with high cost, and a large amount of the industrial waste salt enters a landfill, thereby occupying land resources and directly harming the living environment of human beings. How to remove organic matters in the waste salt, realize clean industrial production, recycle industrial waste salt, change waste into valuable, realize circular economy, is the technical problem that needs to be solved at present.

The prior method for treating organic matters in chemical waste salt comprises the following steps:

1. liquid phase incineration of brine. The melting point of sodium chloride and sodium sulfate is above 800 deg.C, and the liquid phase incineration temperature is far higher than the melting point of sodium chloride and sodium sulfate above 800 deg.C. In the treatment process, a lot of molten salts and cracked organic waste gas escape to a tail gas discharge pipeline in a gaseous state to form coking, the cleaning difficulty is high, and the stable operation of equipment is influenced.

2. High temperature melting method. The service life of the furnace is limited, and splashed molten salt can form more and more hard granite substances on the bottom and the periphery of the furnace, and the furnace needs to be built again. And when the high-temperature molten salt is discharged from the furnace in a liquid state in the disposal process, the temperature is instantly reduced and the material is agglomerated, so that the material receiving machine is constructed into great trouble.

3. The most common waste salt disposal market adopts a rotary kiln high-temperature cracking method. The disadvantages are as follows: the waste salt exists mostly in the form of dust, the sealing performance of the equipment is increasingly poor in the high-temperature operation process of the rotary kiln, and the peripheral environment of the equipment is seriously polluted by the smoke dust and the dust. Secondly, the equipment dynamically operates at high temperature, and the deformation of the bearing, the sealing element and the metal material requires periodic shutdown for maintenance and replacement of accessories, so that the equipment cannot continuously and stably operate. Thirdly, the rotary kiln prevents salt from melting by heating the outside of the shell, although the temperature of salt in the kiln is controlled not to exceed 800 ℃. But powdery salt inevitably cokes on the inner wall of the rotary kiln while operating in high-temperature cracking, because the temperature of the indoor space is controlled to be 600-700 ℃, but the temperature layer of the inner wall of the kiln exceeds 800 ℃, coking cannot be avoided, and molten salt can escape in a gaseous form to block a smoke exhaust pipeline and be irregularly cleaned, so that the stable operation of equipment is directly influenced, and the treatment scale of the equipment is restricted.

4. An internal heating type and external heating type anaerobic carbonization furnace. The problem of dust similar to that of the rotary kiln is inevitable; the high-temperature extension deformation of the metal materials of the bearing, the sealing element and the equipment. Secondly, because the organic matters in the high salt are easy to stick and difficult to decompose in a heated state, the carbonization furnace is often blocked and stopped and cannot normally run.

5. Self-propagating pyrolysis or pyrolysis incineration. Firstly, the waste salt is pretreated to form balls, the particle size is required, the defect that the waste salt balls can only be formed by a disc ball forming machine, the ball forming efficiency is high, the time is long, and the efficiency is low. The pyrolysis process is to ignite the upper layer of the material by an ignition device of the burning section, then exhaust air by negative pressure, so that high-temperature smoke generated by burning starts from the surface layer of the material layer in a self-propagating mode, and gradually moves downwards automatically until the bottom of the material layer finishes the burning of all the material layers, and the work efficiency is low. The utility model discloses a clean high temperature flue gas that oxidation chamber by tail gas treatment provided ignites, high temperature oxidation to belt normal position oxidation unit oxidation section, and the high temperature flue gas is directly penetrated the bed of material by the skip top layer, pyrolysis organic matter, and the work efficiency is high, and the energy consumption is low, and safety in production is more secure. Thirdly, the waste salt with low organic content, such as the polluted salt of sodium chloride in the chlor-alkali industry, can be treated in such a way that the content of the organic content is not high. However, this method cannot dispose of waste salts with high organic content. And fourthly, the temperature reduction flue gas of the self-propagating cooling section is cooled by the dry and preheated flue gas, and the temperature reduction efficiency is low. This scheme is to extract normal atmospheric temperature natural wind with the air-blower, and the cooling is carried out to reverse blowing from the bottom of the bed of material.

6. Domestic sludge, namely municipal sludge and sludge of sewage treatment plants, has the water content of 80-90 percent, high transportation cost and large stacking area, and a landfill blocks a garbage leakage pipe; the air is piled in the open air, bacteria are bred, odor and peculiar smell are emitted, and the air pollution is caused by pollutant particles due to the sun and wind blowing; the organic matter content is high, especially the nitrogen and phosphorus content is high; the pollutants flow into the river along with the river water, and can pollute surface water and underground water.

The current sludge treatment method comprises the following steps: landfill, sea drainage, agriculture, incineration and the like all have some disadvantages: land occupation by landfill; agricultural composting and environmental pollution; high burning and running cost. The methods can not meet the requirements of the existing sludge treatment technology, and the technology of sludge harmless treatment and resource utilization has important practical significance.

7. The oily sludge is oily solid waste generated in the processes of oil exploitation, transportation, refining and oily sewage treatment. The petrochemical industry produces a large amount of tank bottom sludge and pool bottom sludge every year. According to different oil sludge forming reasons, the oil sludge is four types of oil sludge, namely ground oil sludge, tank bottom oil sludge, ground oil spill and oil-containing sludge in an oil refinery. The oil content of the oil sludge is 10-50%, the water content is 40-90%, and the oil-containing sludge contains a large amount of odorous harmful substances such as benzene series, phenols, anthracene, pyrene and the like. If the oily sludge is not treated, the environment is polluted and the resource waste is caused.

At present, the commonly used oily sludge treatment technology in China: firstly, the incineration technology is used for drying and dehydrating, and secondly, the oil sludge content is low, the water content is high, the incineration energy consumption is large, and the operation cost is high. Secondly, the pyrolysis technology firstly needs dehydration and secondly carries out pyrolysis, and because the pyrolysis equipment is in motion, the coking and blockage of oil sludge in a converter (rotary kiln) and auger equipment in the pyrolysis process can cause the equipment to be incapable of normally and continuously running. And thirdly, the cement kiln is cooperatively disposed, so that the popularization and the application are difficult. Solvent extraction and ultrasonic treatment, immature technology and few industrialization cases.

8. The fly ash is a residue collected by a flue gas purification system of a waste incineration plant, belongs to dangerous waste, and contains the most toxic inorganic substance heavy metal and the most toxic organic substance dioxin, wherein the inorganic substance heavy metal comprises lead, chromium, mercury, arsenic and cadmium, and the 5 metals cannot be decomposed in water and are synthesized with other toxins in the water to form organic substances with higher toxicity. Dioxin has great toxicity which is 900 times that of arsenic and is listed as a first-grade carcinogen for human beings.

The treatment method of the fly ash comprises the following steps: chemical treatment method, mixing fly ash with some chemical agents through water, converting heavy metals in fly ash into heavy metals with lower solubility. Secondly, high-temperature treatment is carried out, the fly ash is vitrified, heavy metals are solidified in the slag, the content of the heavy metals is high, and the contained heavy metals and salt are dissolved in water, so that the resource utilization has defects.

The information disclosed in this background section is only for enhancement of understanding of the general background of the invention and should not be taken as an acknowledgement or any form of suggestion that this information constitutes prior art already known to a person skilled in the art.

SUMMERY OF THE UTILITY MODEL

An object of the utility model is to provide a useless processing system of normal position oxidation danger to solve the technical problem who exists among the prior art.

In order to achieve the above purpose, the utility model adopts the following technical scheme:

the utility model provides a useless processing system of normal position oxidation danger, it includes: the system comprises a pretreatment mixing granulation system, a belt type in-situ oxidation device, a flue gas circulation system and a tail gas treatment system; the pretreatment mixing granulation system is connected with the belt type in-situ oxidation device; the material vehicle of the belt type in-situ oxidation device sequentially passes through a drying section, a preheating section, an oxidation section and a cooling section of the flue gas circulating system; the flue gas circulation system is connected with the tail gas treatment system.

Preferably, the exhaust gas treatment system comprises: a second combustion chamber, a semi-dry quenching tower, a Venturi reactor, a bag-type dust collector, a fan, a spray tower, an absorption tower, a chimney, an atomization device, an alkali liquor delivery pump, a clean water tank, a circulation tank, a spray pump, a Roots fan and a star-shaped discharger; the oxidation chamber of the flue gas circulating system is connected with the second combustion chamber; the second combustion chamber, the semi-dry quenching tower, the Venturi reactor, the bag-type dust remover, the fan, the spray tower, the absorption tower and the chimney are sequentially connected; the Roots blower and the Venturi reactor are both connected with the Venturi reactor; the clean water tank is connected with the semi-dry quenching tower through an alkali liquor delivery pump and an atomization device in sequence; the circulating tank is connected with the spray tower through a spray pump.

Preferably, the pre-treatment mixing granulation system comprises: the device comprises a dehydration part, a mixing part, a granulation part, a screening part, a finished product bin part and a belt type in-situ oxidation device which are sequentially arranged along the material conveying direction; the dehydration part is connected with the mixing part; the mixing part is connected with the granulating part; the granulating part is connected with the screening part; the screening part is respectively connected with the material mixing part and the finished product bin part; and the finished product bin part is connected with the belt type in-situ oxidation device.

Preferably, the dehydration part comprises: the device comprises a forklift feeder (travelling crane feeding), a first raw material bin, a first belt scale, a first conveyor, a crusher, a dehydrator and a second conveyor which are arranged in sequence; the forklift feeder is used for feeding materials into an inlet of the raw material bin; a first belt scale is arranged below the outlet of the raw material bin; the output end of the first belt scale is provided with a first conveyor; the output end of the first conveyor is connected with the inlet of the crusher; the lower part of the outlet of the crusher is connected with the inlet of the dehydrator; a second conveyor is arranged below the outlet of the dehydrator; the compounding part includes: the second raw material bin, the third raw material bin, the second belt scale, the stirrer and the third conveyor are sequentially arranged; the output end of the second conveyor is respectively connected with the inlet of the second raw material bin and the inlet of the third raw material bin; a second belt scale is arranged below the outlet of the second raw material bin; a second belt scale is arranged below an outlet of the third raw material bin; the output end of the second belt scale is connected with the inlet of the stirrer; a third conveyor is arranged below the outlet of the stirrer; the granulation section includes: a disc feeder, a granulator and a fourth conveyor; the output end of the third conveyor is connected with the inlet of the disc feeder; a granulator is arranged below the outlet of the disc feeder; a fourth conveyor is arranged below the outlet of the granulator; the screening portion includes: the screening machine, the dryer, the fifth conveyor and the sixth conveyor; the output end of the fourth conveyor is connected with the inlet of the screening machine; the dryer is arranged below a first outlet of the screening machine; a fifth conveyor is arranged below a second outlet of the screening machine; the output end of the fifth conveyor is connected with the inlet of the stirrer; a sixth conveyor is arranged below the outlet of the dryer; the finished product bin portion comprises: the first finished product bin, the second finished product bin and the seventh conveyor; the output end of the sixth conveyor is respectively connected with the inlet of the first finished product bin and the inlet of the second finished product bin; a seventh conveyor is arranged below the outlet of the first finished product bin; a seventh conveyor is arranged below the outlet of the second finished product bin; the output end of the seventh conveyor is connected with the inlet of a distributing device (14) of the belt type in-situ oxidation device.

Preferably, the flue gas circulation system comprises: the device comprises an oxidation chamber, a drying section, a preheating section, an oxidation section and a cooling section; the drying section, the preheating section, the oxidation section and the cooling section are sequentially arranged along the feeding direction; the outlet of the oxidation chamber is connected with the upper end of the oxidation section through an oxidation section air supply pipe and a first heat exchanger; the lower end of the oxidation section is connected with the upper end of the preheating section through an oxidation section exhaust pipe and a first fan; the lower end of the preheating section is connected with the upper end of the drying section through a second fan through a preheating section exhaust pipe; the lower end of the drying section is connected with an inlet of the oxidation chamber through a drying section exhaust pipe via a third fan, a desulfurizer, a dust remover and a second heat exchanger; the upper end of the cooling section is connected with the lower end of the cooling section through a cooling section circulating air pipe through a second heat exchanger and a fourth fan.

Preferably, the upper end of the oxidation chamber is provided with a first outlet and a second outlet; the lower end of the oxidation chamber is provided with an inlet; the oxidation chamber is sequentially provided with a first ignition device and a second ignition device from bottom to top; the first ignition device is used for carrying out first combustion on the flue gas input from the inlet of the oxidation chamber; and the second ignition device is used for carrying out secondary combustion on the flue gas input from the inlet of the oxidation chamber.

Preferably, the first heat exchanger is connected with a first outlet of the oxidation chamber, and the flue gas in the oxidation section air feed pipe is cooled after passing through the first heat exchanger.

Preferably, the second heat exchanger has a first heat exchange channel and a second heat exchange channel; the flue gas in the first heat exchange channel and the flue gas in the second heat exchange channel have a heat exchange effect; the flue gas in the exhaust pipe of the drying section passes through the first heat exchange channel to realize temperature rise; and the flue gas in the cooling section circulating gas pipe is cooled through the second heat exchange channel.

Preferably, the belt type in-situ oxidation apparatus comprises: the device comprises a distributing device, a vertical guide rail, a plurality of skip cars, a head star wheel, a tail star wheel and a flue gas circulating system; the head star wheel is arranged at the head part of the vertical guide rail; the tail star wheel is arranged at the tail part of the vertical guide rail; the vertical guide rail is provided with a plurality of movable skip cars, and the skip cars are connected end to end; the skip car is connected with the head star wheel when passing through the head of the vertical guide rail and moves from the lower layer to the upper layer of the vertical guide rail under the drive of the head star wheel; the skip car is connected with the tail star wheel when passing through the tail part of the vertical guide rail and moves from the upper layer to the lower layer of the vertical guide rail under the drive of the tail star wheel; the upper layer of the vertical guide rail sequentially passes through a drying section, a preheating section, an oxidation section and a cooling section of the flue gas circulating system; the distributing device is positioned in front of the drying section and above the vertical guide rail. Preferably, a material recovery bin is arranged below the material distribution device.

Adopt above-mentioned technical scheme, the utility model discloses following beneficial effect has:

the utility model discloses a belt normal position oxidation method gets rid of the organic matter in the waste salt, has realized getting rid of the organic matter in the danger is useless to reach the danger and abolish "danger" of solving, become "useless" for precious purpose, realized circular economy's effect.

Drawings

In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the embodiments or the technical solutions in the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.

Fig. 1 is a schematic working diagram of a belt type in-situ oxidation apparatus provided in an embodiment of the present invention.

Fig. 2 is a side view of a belt type in-situ oxidation apparatus according to an embodiment of the present invention;

fig. 3 is a sectional view of a belt type in-situ oxidation apparatus provided by an embodiment of the present invention;

fig. 4 is a schematic view of a pretreatment mixing granulation system provided by an embodiment of the present invention;

fig. 5 is a schematic view of a flue gas circulation system according to an embodiment of the present invention.

Detailed Description

The technical solution of the present invention will be described clearly and completely with reference to the accompanying drawings, and obviously, the described embodiments are some, but not all embodiments of the present invention. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.

The following detailed description of the embodiments of the present invention will be made with reference to the accompanying drawings. It should be understood that the description herein is provided for illustration and explanation of the invention and is not intended to limit the invention.

Referring to fig. 1 to 5, the present embodiment provides an in-situ oxidation hazardous waste disposal system, which includes: the system comprises a pretreatment mixing granulation system, a belt type in-situ oxidation device, a flue gas circulation system and a tail gas treatment system; the pretreatment mixing granulation system is connected with the belt type in-situ oxidation device; the trolley 15 of the belt type in-situ oxidation device sequentially passes through the drying section 13, the preheating section 12, the oxidation section 11 and the cooling section 10 of the flue gas circulating system; the flue gas circulation system is connected with the tail gas treatment system.

Example one

This embodiment provides a preliminary treatment compounding granulation system, and it includes: the device comprises a dehydration part 37, a mixing part 38, a granulation part 39, a screening part 40, a finished product bin part 41 and a belt type in-situ oxidation device which are sequentially arranged along the material conveying direction; the dewatering part 37 is connected with the mixing part 38; the mixing part 38 is connected with a granulating part 39; the granulation section 39 is connected to a screening section 40; the screening part 40 is respectively connected with the mixing part 38 and the finished product bin part 41; the finished product bin part 41 is connected with a belt type in-situ oxidation device.

Preferably, the dehydration section 37 comprises: the device comprises a forklift feeder 63, a first raw material bin 42, a first belt scale 43, a first conveyor 44, a crusher 45, a dehydrator 46 and a second conveyor 47 which are arranged in sequence; the forklift feeder 63 is used for feeding materials into an inlet of the raw material bin 42; a first belt scale 43 is arranged below the outlet of the raw material bin 42; the output end of the first belt scale 43 is provided with a first conveyor 44; the output end of the first conveyor 44 is connected with the inlet of a crusher 45; the lower part of the outlet of the crusher 45 is connected with the inlet of the dehydrator 46; a second conveyor 47 is provided below the outlet of the dewatering machine 46.

Preferably, the dehydration engine 46 includes: any one of a centrifugal dehydrator, a stacked screw dehydrator, a paddle dryer, a fluidized bed dryer, and a rotary kiln dryer.

Preferably, the mixing section 38 comprises: a second raw material bin 48, a third raw material bin 49, a second belt scale 50, a stirrer 51 and a third conveyor 52 which are arranged in sequence; the output end of the second conveyor 47 is respectively connected with the inlet of the second raw material bin 48 and the inlet of the third raw material bin 49; a second belt scale 50 is arranged below the outlet of the second raw material bin 48; a second belt scale 50 is arranged below the outlet of the third raw material bin 49; the output end of the second belt scale 50 is connected with the inlet of a stirrer 51; a third conveyor 52 is provided below the outlet of the mixer 51.

Preferably, the blender 51 comprises: any one of a horizontal mixer, a vertical mixer, a double-shaft mixer, a roller mixer, a rotary kiln mixer, and a two-dimensional or three-dimensional mixer.

Preferably, the granulation section 39 comprises: a disc feeder 53, a pelletizer 54, and a fourth conveyor 55; the output end of the third conveyor 52 is connected with the inlet of the disc feeder 53; a granulator 54 is arranged below the outlet of the disc feeder 53; a fourth conveyor 55 is provided below the outlet of the granulator 54.

Preferably, the screening portion 40 comprises: a screening machine 56, a dryer 57, a fifth conveyor 58, a sixth conveyor 59; the output end of the fourth conveyor 55 is connected with the inlet of the screening machine 56; the dryer 57 is arranged below the first outlet of the screening machine 56; a fifth conveyor 58 is arranged below the second outlet of the screening machine 56; the output end of the fifth conveyor 58 is connected with the inlet of the stirrer 51; a sixth conveyor 59 is provided below the outlet of the dryer 57.

Preferably, the screening machine 56 includes: a vibrating screen, a roller cage screen or a roller screen.

Preferably, the dryer 57 includes: any one of a paddle dryer, a fluidized bed dryer, and a rotary kiln dryer.

Preferably, said finished product bin portion 41 comprises: a first finished product bin 60, a second finished product bin 61, and a seventh conveyor 62; the output end of the sixth conveyor 59 is connected with the inlet of the first finished product bin 60 and the inlet of the second finished product bin 61 respectively; a seventh conveyor 62 is arranged below the outlet of the first finished product bin 60; a seventh conveyor 62 is arranged below the outlet of the second finished product bin 61, and the output end of the seventh conveyor 62 is connected with the inlet of the distributing device 14 of the belt type in-situ oxidation device.

Firstly, treating waste salt containing organic matters.

a. High TOC salts, high organic content, which results in the inability to feed or granulate or to oxidize at high temperatures, must be pretreated, high TOC salts to low TOC salts in a weight ratio of 1: 1-10, mixing and stirring, and then granulating.

b. The powdery waste salt and the fine particles are pelletized by a disk pelletizer, but the pelletizing speed is low and the efficiency is low.

c. The disk pelletizer has slow pelletizing speed, can adopt a roller pelletizer, has relatively high speed and high yield.

d. The method is characterized in that powdery waste salt and fine particles are granulated by a double-roller extrusion granulation mode, the particles are oblate, the shape of the particles is not limited, spheres are not required to be formed, and the particle size is 8-30 mm.

e. The salt with the grain size of 3-15 mm can be not granulated.

f. The granulated salt or the salt without pretreatment is directly paved in a skip car, and the stacking height is 150-600 mm.

g. The grate at the bottom of the skip car can be added with a detachable fixed high-temperature-resistant filtering net, and a high-temperature-resistant ball filter core can be laid at the bottom of the net, so that the abrasion of fine particles to the grate and the ash content of waste gas are reduced. The mesh number of the filter screen and the stacking density of the filter element must ensure the ventilation quantity required by waste salt oxidation.

h. The skip car of the system is designed without adding a paving bed charge, and directly paves the granular waste salt. Adding a bedding material reduces the handling capacity and increases the energy consumption per ton.

i. The method for mixing and stirring the high-TOC waste salt and the low-TOC waste salt in proportion and the granulation method are not limited to the use of belt type in-situ oxidation, but also include the use of chain belt type in-situ oxidation, the use of self-propagating treatment, the use of rotary kiln incineration or pyrolysis and the use of carbonization furnace cracking.

(II) domestic sludge.

The water content of the domestic sludge is more than 80 percent, and the pretreatment is to reduce the water content.

a. Plate-frame filter pressing, stacked-screw sludge dewatering, dewatering and drying by a paddle dryer and a roller dryer, and then granulating and sending into a belt type in-situ oxidation device for high-temperature oxidation treatment.

b. Mixing lime and polyaluminium chloride with domestic sludge, performing filter pressing dehydration, adding a proper amount of bran shells and straw biomass fuel to prepare mixed sludge, and feeding the mixed sludge into a belt type in-situ oxidation device for high-temperature oxidation.

And (III) oily sludge.

The water content of the oily sludge is from 30% to more than 80%, and the oily sludge generally comprises oil-in-water, water-in-oil and suspended solids. The oily sludge contains heavy metals such as copper, chromium, mercury and the like, harmful microorganisms, polychlorinated biphenyl, polycyclic aromatic hydrocarbon, phenol, benzene and the like as main organic pollutants.

a. Carrying out quenching and tempering treatment on oil sludge: inorganic flocculant PAC, organic flocculant PAM, filter aid CAO, surfactant, demulsifier and pH regulator, then mechanically dewatering by a membrane filter press until the water content is reduced to below 25%, adding straw, bran shell and biomass fuel, mixing and feeding into a belt type in-situ oxidation device for treatment.

And (IV) waste incineration fly ash.

a. And (3) chemical treatment, namely mixing the fly ash with a chemical agent through water to convert heavy metals in the fly ash into substances with lower solubility and low toxicity. The fly ash can be leached by water, harmful heavy metals such as Cd, Pb, Cu, Zn, Cr and the like with high concentration and salts, and in the second step, acid leaching solution is added into the sludge to separate out the metals and salts to the maximum extent. The saline water solution can be refined by evaporation and crystallization.

b. The fly ash subjected to chemical pretreatment is made into particles with the particle size of 5-20 mm, the particles are sent to belt type in-situ oxidation to be subjected to high-temperature oxidation, heavy metal pollutants are effectively fixed, dioxin pollutants are thoroughly decomposed and destroyed, and the product has the characteristics of high-strength lightweight aggregate through high-temperature oxidation and can be used for casting common concrete and paving roadbed cushions.

c. The fly ash subjected to chemical treatment is matched with coke powder to prepare particles with the particle size of 5-20 mm, and the particles are sent to belt type in-situ oxidation. The ignition temperature is normally set above 900 deg.C, the burning temperature can reach 1300 deg.C at most, and the fly ash is melted. The addition of coke powder reduces energy consumption. The molten glass fixes heavy metals therein, and the leaching rate is extremely low.

In this embodiment, the working principle of the pretreatment mixing granulation system is as follows: the method comprises the steps of putting ton bags of waste salt into a first raw material bin 42 by a forklift feeder 63 (or a travelling crane), conveying the ton bags of waste salt to a crusher 45 after metering by a first belt scale 43, dewatering and drying by a dewaterer 46 (comprising a centrifugal dewaterer, a stacked screw type dewaterer, a paddle dryer, a fluidized bed dryer and a rotary kiln dryer), conveying different salts with the water content of below 15% to a second raw material bin 48 and a third raw material bin 48 respectively, conveying the second belt scale 50 after weighing to a stirrer 51 for stirring (comprising a horizontal stirrer, a vertical stirrer, a double-shaft stirrer, a roller stirrer and a rotary kiln type stirrer), conveying the uniformly mixed salts to a disc feeder 53, conveying the disc feeder 54 for granulating, conveying the disc feeder 56 for sieving (comprising a vibrating screen and a rolling cage sieve), conveying the granular salt and the powder salt with the particle size of above 5mm to the stirrer 51 for mixing and re-granulating, the salt with the particle size of more than 8-10mm is dried by a dryer 57 (comprising a paddle dryer, a fluidized bed dryer and a rotary kiln dryer) and then is conveyed to finished product bins 60 and 61 to wait for being sent to a distributing device 14 and a skip 15 of a belt type in-situ oxidation device 32, so that all processes of pretreating, mixing and granulating are completed.

Example two

In this embodiment, on the basis of the first embodiment, a belt type in-situ oxidation apparatus is provided, which includes: the device comprises a distributing device 14, a vertical guide rail, a plurality of material trucks 15, a head star wheel 16, a tail star wheel 17 and a smoke circulating system; the head star wheel 16 is arranged at the head part of the vertical guide rail; the tail star wheel 17 is arranged at the tail part of the vertical guide rail; the vertical guide rail is provided with a plurality of movable skip cars 15, and the skip cars 15 are connected end to end; the skip car 15 is connected with the head star wheel 16 when passing through the head of the vertical guide rail, and moves from the lower layer to the upper layer of the vertical guide rail under the driving of the head star wheel 16; the skip car 15 is connected with the tail star wheel 17 when passing through the tail part of the vertical guide rail, and moves from the upper layer to the lower layer of the vertical guide rail under the driving of the tail star wheel 17; the upper layer of the vertical guide rail sequentially passes through a drying section 13, a preheating section 12, an oxidation section 11 and a cooling section 10 of a flue gas circulating system; the distributing device 14 is located in front of the drying section 13 and above the vertical guide rail. Preferably, a material recovery bin 26 is arranged below the distributing device 14.

Preferably, the head star wheel 16 constitutes a driving wheel of the belt type in-situ oxidation device; the tail star wheel 17 forms a driven wheel of the belt type in-situ oxidation device; the head star wheel 16 is connected with a speed reducer and a motor.

Preferably, the vertical guide rail includes: an upper guide rail, a lower guide rail, a head arc-shaped guide rail 34 and a tail arc-shaped guide rail 35; the upper guide rail, the lower guide rail, the head arc-shaped guide rail 34 and the tail arc-shaped guide rail 35 form a vertical closed vertical guide rail.

The headrail includes: the first upper-running single rail 102, the first upper-running inner rail 103, the second upper-running inner rail 104 and the second upper-running single rail 105 are sequentially arranged in parallel; the down guide includes: a first descending single rail and a second descending single rail which are arranged in parallel; the head arc rail 34 includes: the first head arc-shaped monorail and the second head arc-shaped monorail are arranged in parallel; the upper end of the first head arc-shaped monorail is connected with an upper layer linear monorail, and the lower end of the first head arc-shaped monorail is connected with a lower layer linear monorail; the upper end of the second head arc-shaped single rail is connected with an upper layer linear single rail, and the lower end of the second head arc-shaped single rail is connected with a lower layer linear single rail; the tail arc guide rail 35 includes: the first tail arc-shaped monorail and the second tail arc-shaped monorail are arranged in parallel; the upper end of the first tail arc-shaped single rail is connected with an upper layer linear single rail, and the lower end of the first tail arc-shaped single rail is connected with a lower layer linear single rail; the upper end of the second tail arc-shaped single rail is connected with an upper layer linear single rail, and the lower end of the second tail arc-shaped single rail is connected with a lower layer linear single rail; the first upper monorail 102 is located above the first lower monorail; the head end of the first upper monorail 102 is positioned below the upper layer linear monorail of the first head arc monorail; the tail end of the first upper monorail 102 is positioned below the lower linear monorail of the first tail arc monorail; the head end of the first descending single rail is in butt joint with the lower linear single rail of the first head arc-shaped single rail; the tail end of the first descending monorail is butted with a lower linear monorail of the first tail arc monorail; the head end of the second upper monorail 105 is positioned below the upper layer linear monorail of the second head arc monorail; the tail end of the second upper monorail 105 is positioned below the lower linear monorail of the second tail arc monorail; the head end of the second descending monorail is butted with the lower layer linear monorail of the second head arc monorail; the tail end of the second descending monorail is butted with a lower-layer linear monorail of the second tail arc monorail;

a side roller 31 of the skip car 15 circularly moves along the inner side surface of the first head arc-shaped monorail, the upper surface of the first upper-going monorail 102, the inner side surface of the first tail arc-shaped monorail and the upper surface of the first lower-going monorail; and rollers on the other side of the skip 15 circularly move along the inner side surface of the second head arc-shaped monorail, the upper surface of the second upper-moving monorail 105, the inner side surface of the second tail arc-shaped monorail and the upper surface of the second lower-moving monorail.

Preferably, the skip 15 comprises: a skip base, two skip outer side plates 15 and four rollers 31; two sides of the skip car base are respectively provided with a skip car outer side plate 15; the skip outer side plate 15 and the skip base enclose an accommodating space for placing materials; the two rollers 31 are respectively arranged on the outer side of the front part of the skip car base through rotating shafts; the two rollers 31 are respectively arranged on the outer side of the rear part of the skip car base through rotating shafts; a section of meshing section is reserved between the roller 31 and the outer side of the skip base on the rotating shaft; the meshing section is used for meshing with tooth gaps of the head star wheel 16 and the tail star wheel 17 to realize the propelling of the skip car.

Preferably, two mounting grooves are symmetrically formed in two sides of the bottom of the skip car base; the interior of the mounting groove is connected with a sealing structure 36 through a spring, and the sealing structure 36 is used for being pressed on the first upper inner rail 103 and the second upper inner rail 104; two transverse plates 100 are symmetrically arranged on two outer sides of the skip car base.

Preferably, a detachable filter screen is arranged on the skip car base; the skip car base is provided with a filter ball (steel ball) on a filter screen. The mesh number of the filter screen and the stacking density of the filter element must ensure the ventilation quantity required by waste salt oxidation. It should be noted that the skip 15 can also be designed to directly lay the waste granular salt without adding a bed charge. Adding a bedding material reduces the handling capacity and increases the energy consumption per ton.

The working principle of the embodiment is as follows:

the empty skip 15 enters the lower part of the distributing device 14 to be spread along the direction indicated by an arrow driving the head star wheel 16, the spread skip 15 sequentially enters the drying section 13, the preheating section 12, the oxidation section 11 and the skip 15 after oxidation treatment of the cooling section 10 along an upward straight guide rail of the belt type in-situ oxidation device 32 to enter the discharging area of the tail star wheel 17 to be discharged, and then the empty skip is hung upside down on a downward straight guide rail of the belt type in-situ oxidation device 32 to sequentially move forward to the distributing area of the head star wheel 16 to wait for spreading, and then the empty skip enters the next working cycle.

EXAMPLE III

On the basis of the second embodiment, the present embodiment provides a flue gas circulation system. The second embodiment includes the contents of the first embodiment, and the same parts are not described again. The flue gas circulation system includes: an oxidation chamber 8, a drying section 13, a preheating section 12, an oxidation section 11 and a cooling section 10; the drying section 13, the preheating section 12, the oxidation section 11 and the cooling section 10 are sequentially arranged along the feeding direction; the upper layer of the vertical guide rail sequentially passes through a drying section 13, a preheating section 12, an oxidation section 11 and a cooling section 10 of a flue gas circulating system; the outlet of the oxidation chamber 8 is connected with the upper end of an oxidation section 11 through an oxidation section air supply pipe 1 and a first heat exchanger 9; the lower end of the oxidation section 11 is connected with the upper end of the preheating section 12 through an oxidation section exhaust pipe 2 by a first fan 27; the lower end of the preheating section 12 is connected with the upper end of the drying section 13 through a second fan 28 by a preheating section exhaust pipe 3; the lower end of the drying section 13 is connected with the inlet of the oxidation chamber 8 through the drying section exhaust pipe 4, the third fan 29, the desulfurizer 6, the dust remover 33 and the second heat exchanger 7; the upper end of the cooling section 10 is connected with the lower end of the cooling section 10 through a cooling section circulating air pipe 5 via a second heat exchanger 7 and a fourth fan 30.

Preferably, the upper end of the oxidation section 11 is provided with an oxidation section air supply cover 24; the upper end of the oxidation section air supply cover 24 is connected with the oxidation section air supply pipe 1; an oxidation section induced air cover 20 is arranged at the lower end of the oxidation section 11; the lower end of the oxidation section induced draft cover 20 is connected with the oxidation section exhaust pipe 2; the oxidation section 11 is provided with a chamber for allowing the skip car to pass through and oxidizing the material in the skip car.

Specifically, the oxidation section air supply cover 24 is positioned above the skip car and covers the space above the skip car; preferably, the lower edges of the two side walls of the oxidation zone air supplying cover 24 are provided with grooves, the grooves are internally provided with a floating plate, the bottom of the floating plate is provided with a sealing part with a circular section and is used for being in sliding sealing contact with the transverse plate 100 on the base of the skip car, so that an upper chamber which allows the skip car to pass through and is sealed is formed above the skip car so as to prevent high-temperature gas from overflowing. Meanwhile, the oxidation section induced draft cover 20 is arranged between the first upper inner rail 103 and the second upper inner rail 104 on the skip base; two mounting grooves are symmetrically arranged on two sides of the bottom of the skip car base; the inside of mounting groove has seal structure 36 through spring coupling, seal structure 36 is used for the crimping on first interior rail 103 of going upward, the second inner rail 104 of going upward, also forms a lower chamber that allows the skip to pass through and seal like this in the below of skip to whole upper chamber, skip, lower chamber form a dynamic confined space jointly.

Preferably, a preheating section air supply cover 23 is arranged at the upper end of the preheating section 12; the upper end of the preheating section air supply cover 23 is connected with the oxidation section exhaust pipe 2; the lower end of the preheating section 12 is provided with a preheating section induced draft cover 19; the lower end of the preheating section induced draft hood 19 is connected with the preheating section exhaust pipe 3; the preheating section 12 is provided with a chamber for allowing the skip car to pass through and preheating the material in the skip car.

Specifically, the preheating section air supply cover 23 is positioned above the skip car and covers the space above the skip car; preferably, the lower edges of the two side walls of the preheating section air supplying cover 23 are provided with grooves, the grooves are internally provided with a floating plate, the bottom of the floating plate is provided with a sealing part with a circular section for sliding and sealing contact with the transverse plate 100 on the base of the skip car, so that an upper chamber which allows the skip car to pass through and is sealed is formed above the skip car, and high-temperature gas is prevented from overflowing. Meanwhile, the air induction cover 19 of the preheating section is arranged between the first upper inner rail 103 and the second upper inner rail 104 on the base of the skip car; two mounting grooves are symmetrically arranged on two sides of the bottom of the skip car base; the inside of mounting groove has seal structure 36 through spring coupling, seal structure 36 is used for the crimping on first interior rail 103 of going upward, the second inner rail 104 of going upward, also forms a lower chamber that allows the skip to pass through and seal like this in the below of skip to whole upper chamber, skip, lower chamber form a dynamic confined space jointly.

Preferably, a drying section air supply cover 22 is arranged at the upper end of the drying section 13; the upper end of the drying section air supply cover 22 is connected with the preheating section exhaust pipe 3; the lower end of the drying section 13 is provided with a drying section induced air cover 18; the lower end of the drying section induced air cover 18 is connected with the drying section exhaust pipe 4; a chamber for allowing the skip car to pass through and drying the materials in the skip car is formed in the drying section 13.

Specifically, the drying section air supply cover 22 is positioned above the skip car and covers the space above the skip car; preferably, the lower edges of the two side walls of the drying section air supplying cover 22 are provided with grooves, the grooves are internally provided with a floating plate, the bottom of the floating plate is provided with a sealing part with a circular section for sliding and sealing contact with a transverse plate 100 on the base of the skip car, so that an upper chamber which allows the skip car to pass through and is sealed is formed above the skip car to prevent high-temperature gas from overflowing. Meanwhile, the drying section induced air cover 18 is arranged between the first upper inner rail 103 and the second upper inner rail 104 on the skip base; two mounting grooves are symmetrically arranged on two sides of the bottom of the skip car base; the interior of the mounting groove is connected with a sealing structure 36 through a spring, the sealing structure 36 is used for being pressed on the first upper inner rail 103 and the second upper inner rail 104, and a lower chamber which allows the skip car to pass through and is sealed is formed below the skip car, so that the whole upper chamber, the skip car and the lower chamber form a dynamic sealing space together.

Preferably, the upper end of the cooling section 10 is provided with a cooling section air supply cover 25; the lower end of the cooling section 10 is provided with a cooling section air distribution box 21; a cavity allowing the skip car to pass through and cooling the materials in the skip car is formed in the cooling section air supply cover 25; the upper end of the cooling section air supply cover 25 is connected with the lower end of the cooling section air distribution box 21 through a cooling section circulating air pipe 5 via a second heat exchanger 7 and a fourth fan 30. Specifically, the cooling section air supply cover 25 is positioned above the skip car and covers the space above the skip car; preferably, the lower edges of the two side walls of the cooling section air supplying cover 25 are provided with grooves, the grooves are internally provided with a floating plate, the bottom of the floating plate is provided with a sealing part with a circular section for sliding and sealing contact with the transverse plate 100 on the base of the skip car, so that an upper chamber which allows the skip car to pass through and is sealed is formed above the skip car, and high-temperature gas is prevented from overflowing. Meanwhile, the cooling section air distribution box 21 is arranged between the first upper inner rail 103 and the second upper inner rail 104 on the base of the skip car; two mounting grooves are symmetrically arranged on two sides of the bottom of the skip car base; the inside of mounting groove has seal structure 36 through spring coupling, seal structure 36 is used for the crimping on first interior rail 103 of going upward, the second inner rail 104 of going upward, also forms a lower chamber that allows the skip to pass through and seal like this in the below of skip to whole upper chamber, skip, lower chamber form a dynamic confined space jointly.

Preferably, the upper end of the oxidation chamber 8 is provided with a first outlet and a second outlet; the lower end of the oxidation chamber 8 is provided with an inlet; the oxidation chamber 8 is sequentially provided with a first ignition device and a second ignition device from bottom to top; the first ignition device is used for carrying out first combustion on the flue gas input from the inlet of the oxidation chamber 8; the second ignition device is used for carrying out secondary combustion on the flue gas input from the inlet of the oxidation chamber 8. It can be understood that the oxidation chamber 8 is provided with an upper ignition device and a lower ignition device, natural gas and combustion-supporting air are used for burning the micromolecule organic waste gas fed in from the front end, the burning-out rate of organic matters reaches more than 99.9 percent, and dioxin is also fully decomposed. One part of the high-temperature flue gas after oxidative decomposition is sent to a rear-end secondary combustion chamber to be subjected to incineration and other tail gas treatment processes at the temperature of more than 1100 ℃, and most other high-temperature flue gas after purification treatment at the temperature of 850 ℃ is cooled by a first heat exchanger 9 and then is pumped into an oxidation section air supply hood 24 by a first induced draft fan 27. Of course, in addition to this, the oxidation chamber 8 can also be provided with one ignition device, or another number of ignition devices.

Preferably, the first heat exchanger 9 is connected with a first outlet of the oxidation chamber 8, and the flue gas in the oxidation section air feed pipe 1 is cooled after passing through the first heat exchanger 9. The first heat exchanger 9 can be flexibly selected according to the requirements. For example: a continuously circuitous radiating pipe is arranged between an inlet and an outlet of the first heat exchanger 9; the inside of the radiating pipe is communicated with an air supply pipe 1 of the oxidation section. The outside of the heat dissipation pipe is water cooling medium or air cooling medium.

Preferably, the second heat exchanger 7 has a first heat exchange channel and a second heat exchange channel; the flue gas in the first heat exchange channel and the flue gas in the second heat exchange channel have a heat exchange effect; the flue gas in the exhaust pipe 4 of the drying section passes through the first heat exchange channel to realize temperature rise; and the flue gas in the cooling section circulating gas pipe 5 is cooled through the second heat exchange channel. Likewise, the choice of the second heat exchanger 7 is also various, for example: the first heat exchange channel is a space inside the shell of the second heat exchanger 7 and outside the second heat exchange channel; the second heat exchange tube is a continuous circuitous radiating tube.

The working principle of the embodiment is as follows:

the independent oxidation chamber 8 is set to 850 ℃, natural gas is used for ignition, organic waste gas after oxidative decomposition sent by the front-end oxidation section 11, the preheating section 12 and the drying section 13 is incinerated, most of the flue gas after the clean treatment of the oxidation chamber 8 enters the air supply hood 24 of the oxidation section through the air supply pipe 1 of the oxidation section by the first fan 27, the high-temperature flue gas generated by the oxidation section 11 is pumped to the preheating air supply cover 23 of the preheating section 12 through the oxidation section induced air cover 20 and the oxidation section exhaust pipe 2 by the first fan 27, the high-temperature flue gas generated in the preheating section 12 is pumped to the drying section air supply hood 22 through the preheating section air induction hood 19 and the preheating section exhaust pipe 3 by the second fan 28, and the hot flue gas dried and cooled in the drying section 13 is pumped out by the third fan 29 through the drying section induced draft cover 18 and the drying section exhaust pipe 4, then is heated by the desulfurizer 6, the dust remover 33 and the second heat exchanger 7, and then is sent to the oxidation chamber 8 for incineration. The cooling of the cooling section 10 is realized by reversely blowing low-temperature air of the air distribution box 21 of the cooling section from bottom to top to the surface layer of the material at the bottom layer of the skip material of the cooling section 10 by a fourth fan 30 (the fourth fan is a roots fan), and after the cooling air cools the high-temperature material, the hot air which absorbs heat and is heated is continuously cooled by the second heat exchanger 7 and then is recycled.

According to the flue gas circulation system, an ignition system is not arranged on the belt type in-situ oxidation machine, but an oxidation chamber of a tail gas treatment system is used, natural gas passes through a burner nozzle and is matched with natural wind to heat up to 850 ℃ so as to burn organic waste gas coming from the belt type in-situ oxidation. After the clean treatment of the oxidation chamber, part of the 850 ℃ high-temperature flue gas enters a secondary combustion chamber for further purification treatment at 1100 ℃ through a main induced draft fan of tail gas; and the other part of the flue gas is subjected to waste heat utilization. And the high-temperature flue gas reaching the proper temperature and the proper air quantity of the oxidation section enters the belt type in-situ oxidation flue gas circulating system through the draught fan pipeline, the air draft cover and the heat preservation cover. Provides a heat source for the ignition of hazardous waste and the oxidative decomposition of organic matters in the oxidation skip car.

The method for recycling the high-temperature flue gas is particularly suitable for treating chemical waste salt containing organic matters.

In the process of treating chemical waste salt, domestic sludge, oily sludge and fly ash generated by refuse incineration, besides the method of using the high-temperature flue gas circulation, an ignition device can also be arranged at the upper part of the upper section heat-insulating cover of the skip car of the belt type in-situ oxidation device, and the ignition device is made into a hot air generating device by utilizing the boiled gas and adding a proper amount of natural air so as to provide a flue gas heat source with a proper temperature and a proper air volume for oxidative decomposition.

The smoke circulating system can be additionally provided with an online ignition device which can be horizontally installed or vertically installed, so that a fire source is ensured not to be in direct contact with materials. The temperature set by the on-line ignition device is not limited to 850 ℃ and 1100 ℃, and can be set according to the oxidation temperature required by different hazardous waste disposals, and the flue gas finally recycled is sent into a secondary combustion chamber of a tail gas system for high-temperature purification treatment at 1100 ℃. The position of the on-line ignition device is set to be capable of entering the oxidation section area at the preheating section to be provided with the ignition device, and the ignition device and the matched hot air generating device are arranged at the oxidation section at the same time, so that the hot air with the required temperature for the oxidation of the dangerous waste is provided on line, and meanwhile, the hot air circulating pipeline for utilizing the waste heat of the organic waste gas generated by the oxidation of the dangerous waste is burnt on line:

the method comprises the following steps of firstly, oxidizing section → preheating section → drying section → part of the tail gas enters the oxidizing section (ignition burning) → part of the tail gas enters the tail gas purification system.

Cooling → oxidation (ignition burning). The cooled hot flue gas is sent to an ignition device of an oxidation section to supplement the heat of the air required by incineration, and the consumption of the natural gas required by incineration is reduced.

Cooling → drying → oxidizing (ignition burning). The cooled hot flue gas can be circulated in the mode of II, or can be directly sent to the drying section first, the materials are heated, and then the materials are sent to the oxidation ignition device after the moisture is removed.

Adopting the flue gas circulation method of the third step, the circulation method section of the first step is adjusted to the following method:

oxidation section → preheating section → partial oxidation section (ignition burning) → partial entering exhaust gas purification system

The above two ignition modes of the flue gas circulating systems can be used as a pipeline system for one-time or two-time or four-time quantity sequential forward cyclic utilization in a specific oxidation section, a preheating section and a drying section according to different decomposition temperatures of different hazardous waste organic matters.

The drying section, the preheating section and the oxidation section of the belt type in-situ oxidation device use temperature-resistant and pressure-resistant induced draft fans for air draft; the cooling section is blown by a temperature-resistant Roots blower. The air draft cover at the lower end of the belt type in-situ oxidation device is connected with the sliding track of the belt type skip car, and the air ducts of the expansion joints are additionally arranged, so that the extension deformation of the air draft cover and the air draft pipe caused by the high temperature of smoke is avoided, and the sealing effect of the air draft cover and the track at the lower end of the skip car is influenced. Each draft hood is provided with a thermocouple for measuring temperature, an oxygen analyzer for measuring oxygen content and a pressure transmitter for measuring negative pressure. All fans of the system are adjustable in frequency conversion, and energy consumption is saved. The bottom of the material layer of the skip car does not need to be added with a bedding material. The thickness of the material layer in the skip car is 150-1200 mm. The thickness of the waste salt layer is 150-600 mm. The time required from drying to preheating to oxidation of the belt type in-situ oxidation is 50-160 minutes, and the time of the cooling period is within 20 minutes. The negative pressure for oxidative decomposition of chemical waste salt is preferably controlled at 1000-12000Pa and the oxidative decomposition temperature is 600-800 ℃. The oxidative decomposition temperature of other low melting point salts is adjusted to be lower than the melting temperature of the salt. The oxidation temperature of the domestic sludge, the oil sludge and the fly ash is 500-1300 ℃. In the material spreading section, a raw material recovery bin is designed below the skip car. And a material recovery device after treatment is arranged below the discharging section and below the empty wagon return stroke, and comprises a recovery bin and a conveying system. The vertical belt structure is superior to the vertical chain belt structure, so that the sealing performance is good, the transmission is stable, the fault is small, and the service life is long. The belt type in-situ oxidation system calculates the areas of the drying section, the preheating section, the oxidation section and the cooling section according to the output of different hazardous waste disposals and the required air volume, temperature and time in strict proportion.

In summary, the ignition device is not arranged on the belt-type in-situ oxidation device of the embodiment, the heat source is provided by an independent oxidation chamber of the tail gas treatment system, the temperature of the flue gas at the outlet of the oxidation chamber is 800-900 ℃, the flue gas is pumped to the upper wind hood of the oxidation section of the belt-type oxidation device by the induced draft fan, and the negative pressure is controlled to be 1000-10000Pa by adopting a negative pressure air draft mode. The hot air at 800 ℃ directly penetrates to the bottom layer of the material from the surface layer of the material of the skip car, so that the hazardous waste organic matters are oxidized and decomposed to form gas compounds which are pumped out by the induced draft fan to separate from the oxidation skip car, N, S-containing molecules and other pollution molecules are absorbed by a smoke system, and the organic matters in the hazardous waste are effectively separated and treated, so that the hazardous waste is decomposed into 'hazardous'. The skip car which is oxidized and then removes organic matters moves forwards to a cooling section to be cooled and moves forwards to a tail wheel section, the skip car tilts and overturns to discharge, so that hazardous wastes become industrial byproducts and enter a subsequent resource utilization process. The high-temperature flue gas in the oxidation section is pumped to an air supply cover at the upper end of a skip car in the preheating section from the bottom of the oxidation section by an exhaust fan, and materials in the skip car are preheated. And continuously moving the loaded and preheated dangerous waste material vehicle to an oxidation section. The high-temperature flue gas in the preheating section is pumped to an air supply cover at the upper part of the drying section from an induced draft cover at the bottom of the preheating end by an exhaust fan. And (4) the material trolley coming from the material distribution section enters a drying section, and surface water and crystal water in the material are evaporated after the temperature of the material is raised. And continuously moving the dried dangerous waste material vehicle forwards to a preheating section. And the cooling of the material in the cooling section is realized by blowing the air of an air distribution box below the skip car in the cooling section to the surface of the material layer from the bottom of the skip car by a blower to cool. And the skip car for loading and removing the organic matter materials leaves the cooling section and moves forwards to the unloading area of the tail star wheel for unloading. The normal temperature wind of the cooling section reduces the temperature of the high-temperature material in the oxidation section, the temperature of the normal temperature wind is also increased, and the heated cooling wind heats the flue gas discharged from the drying section by using the heat exchanger. The cooling air is always recycled.

Example four

On the basis of the first embodiment, the present embodiment provides an exhaust gas treatment system, which includes: a secondary combustion chamber 101, a semi-dry quenching tower 102, a venturi reactor 103, a bag-type dust remover 104, a fan 105, a spray tower 106, an absorption tower 107, a chimney 108, an atomization device 109, an alkali liquor delivery pump 110, a clean water tank 111, a circulating tank 112, a spray pump 113, a roots fan 114 and a star discharger 115; the oxidation chamber 8 of the flue gas circulating system is connected with the secondary combustion chamber 101; the secondary combustion chamber 101, the semi-dry quenching tower 102, the venturi reactor 103, the bag-type dust collector 104, the fan 105, the spray tower 106, the absorption tower 107 and the chimney 108 are sequentially connected; the Roots blower 114 and the Venturi reactor 103 are both connected with the Venturi reactor 103; the clean water tank 111 is connected with the semi-dry quenching tower 102 through an alkali liquor delivery pump 110 and an atomization device 109 in sequence; the circulation tank 112 is connected to the spray tower 106 by a spray pump 113.

In this embodiment, after the hazardous waste is subjected to the belt-type in-situ oxidation, the organic substances are oxidized and decomposed into gaseous compounds, such as CO and SO ₂ 、NO、NO ₂ 、NOX、VOCs、O ₂ And water vapor and the like enter the flue gas treatment system along with flue gas, are subjected to dust removal and desulfurization at first, are heated by the heat exchanger and are sent to the oxidation chamber for incineration treatment at 850 ℃, the VOC damage removal rate can reach 99.9% at the temperature, and dioxin is fully decomposed. And a part of flue gas enters the belt type oxidation heat energy for cyclic utilization, and a part of flue gas enters the secondary combustion chamber to be heated to 1100 ℃ so as to ensure that dioxin is thoroughly decomposed. Meets the national hazardous waste incineration standard and meets the environmental evaluation requirement. The flue gas with the temperature of 1100 ℃ stays in the secondary combustion for more than 2S, the flue gas is led out of the secondary combustion chamber by the induced draft fan, the SNCR denitration device is arranged on the gas outlet pipeline, ammonia water with the concentration of 10-15% or 15% of urea reducing agent is used for denitration, and the denitration and the nitrogen oxide are reduced into harmless nitrogen and water. And the waste heat of the denitrated flue gas is utilized and then is reduced to 550-600 ℃, and the denitrated flue gas is sent to a semi-dry quenching tower and is reduced to 200 ℃ in 1S, so that the generation of dioxin is inhibited. The flue gas enters a dry type reaction device. The slaked lime powder and the activated carbon powder are sprayed into a Venturi flue in front of a bag type dust collector to further remove acidic substances in the flue gas and adsorb most harmful substances such as dioxin and the like. The bag-type dust remover removes dust with a particle size of more than 0.05um and a dust removal rate of more than 99%.

The flue gas enters a spray tower and an absorption tower after passing through a bag-type dust collector and a draught fan, secondary washing absorption is adopted, the removal efficiency of acidic substances in the flue gas is ensured, and the flue gas is washed to remove acidic gases such as hydrogen chloride, sulfur dioxide and the like. And the wastewater from the washing tower enters an adjusting tank after being precipitated, and is pumped into the washing tower after the pH value is adjusted for recycling. The temperature of a flue gas outlet is about 40 ℃, the flue gas is discharged at high pressure through a chimney, and the chimney is provided with a lightning rod, flue gas online detection and the like, so that the treatment and discharge of the belt type in-situ oxidation whole system are ensured to meet the environmental protection requirement.

EXAMPLE five

The present embodiment provides a method for disposing in-situ oxidation hazardous waste, which adopts the in-situ oxidation hazardous waste disposal system in the first to fourth embodiments. The disposal object of the in-situ oxidation hazardous waste disposal system is chemical waste salt containing organic matters. The method comprises the steps of putting ton bags of waste salt into a first raw material bin 42 by a forklift feeder 63 (or a travelling crane), conveying the ton bags of waste salt to a crusher 45 after metering by a first belt scale 43, dewatering and drying by a dewaterer 46 (comprising a centrifugal dewaterer, a stacked screw type dewaterer, a paddle dryer, a fluidized bed dryer and a rotary kiln dryer), conveying different salts with the water content of below 15% to a second raw material bin 48 and a third raw material bin 48 respectively, conveying the second belt scale 50 after weighing to a stirrer 51 for stirring (comprising a horizontal stirrer, a vertical stirrer, a double-shaft stirrer, a roller stirrer and a rotary kiln type stirrer), conveying the uniformly mixed salts to a disc feeder 53, conveying the disc feeder 54 for granulating, conveying the disc feeder 56 for sieving (comprising a vibrating screen and a rolling cage sieve), conveying the granular salt and the powder salt with the particle size of above 5mm to the stirrer 51 for mixing and re-granulating, the salt with the particle size of more than 8-10mm is dried by a dryer 57 (comprising a paddle dryer, a fluidized bed dryer and a rotary kiln dryer) and then is conveyed to finished product bins 60 and 61 to wait for being sent to a distributing device 14 and a skip 15 of a belt type in-situ oxidation device 32, so that all processes of pretreating, mixing and granulating are completed.

2-15 mm granular salt does not need to be granulated; crushing the hardened salt blocks and large-particle salt with the particle size of more than 25mm, and then granulating; the powdered salt is granulated. The particle size of the waste salt granulation is controlled to be 5-20 mm, then the waste salt granulation is conveyed to a distributing device to pave a skip 15, and the thickness of the paved material is controlled to be 150-700 mm.

The empty skip 15 enters the lower part of the distributing device 14 along the direction indicated by the arrow of the driving head star wheel 16 for spreading, the spread skip 15 sequentially enters the drying section 13, the preheating section 12, the oxidation section 11 and the skip 15 after oxidation treatment of the cooling section 10 along the upward straight guide rail of the belt type in-situ oxidation device 32, enters the discharging area of the tail star wheel 17 for discharging, then is hung upside down on the downward straight guide rail of the belt type in-situ oxidation device 32, sequentially forwards moves to the distributing area of the head star wheel 16 for waiting for spreading, and enters the next working cycle.

The independent oxidation chamber 8 is set to 850 ℃, natural gas is used for ignition, organic waste gas after oxidative decomposition sent by the front-end oxidation section 11, the preheating section 12 and the drying section 13 is incinerated, most of the clean treated smoke of the oxidation chamber 8 enters the air supply hood 24 of the oxidation section through the oxidation section air supply pipe 1 by the first fan 27, and the other part of the oxidation chamber 8 is sent to the rear-end secondary combustion chamber to carry out incineration and other tail gas treatment processes above 1100 ℃. High-temperature flue gas generated by the oxidation section 11 is pumped to a preheating air supply cover 23 of the preheating section 12 through an oxidation section air induction cover 20 and an oxidation section exhaust pipe 2 by a first fan 27, high-temperature flue gas generated by the preheating section 12 is pumped to a drying section air supply cover 22 through a preheating section air induction cover 19 and a preheating section exhaust pipe 3 by a second fan 28, and hot flue gas which is dried and cooled in the drying section 13 is pumped out through a drying section air induction cover 18 and a drying section exhaust pipe 4 by a third fan 29, then is heated by a dust remover 33, a desulfurizer 6 and a second heat exchanger 7, and then is sent to the oxidation chamber 8 for incineration. The cooling of the cooling section 10 is realized by reversely blowing low-temperature air of the air distribution box 21 of the cooling section from bottom to top to the surface layer of the material at the bottom layer of the skip material of the cooling section 10 by a fourth fan 30 (the fourth fan is a roots fan), and after the cooling air cools the high-temperature material, the hot air which absorbs heat and is heated is continuously cooled by the second heat exchanger 7 and then is recycled.

After the hazardous waste is subjected to belt type in-situ oxidation, organic matters are oxidized and decomposed into gas compounds such as CO and SO ₂ 、NO、NO ₂ 、NOX、VOCs、O ₂ And water vapor and the like enter the flue gas treatment system along with flue gas, are subjected to dust removal and desulfurization at first, are heated by the heat exchanger and are sent to the oxidation chamber for incineration treatment at 850 ℃, the VOC damage removal rate can reach 99.9% at the temperature, and dioxin is fully decomposed. And a part of flue gas enters a belt type oxidation heat energy for cyclic utilization, and a part of flue gas enters a secondary combustion chamber to be heated to 1100 ℃, so that the dioxin is ensured to be thoroughly decomposed. Meets the national hazardous waste incineration standard and meets the environmental evaluation requirement. 1100 deg.CThe flue gas stays in the secondary combustion for more than 2S, is led out of the secondary combustion chamber by the induced draft fan, and an SNCR denitration device is arranged on the gas outlet pipeline and is denitrated by ammonia water with the concentration of 10-15% or 15% of urea reducing agent, and the denitrated ammonia water and the nitric oxide are reduced into harmless nitrogen and water. And the waste heat of the denitrated flue gas is utilized and then is reduced to 550-600 ℃, and the denitrated flue gas is sent to a semi-dry quenching tower and is reduced to 200 ℃ in 1S, so that the generation of dioxin is inhibited. The flue gas enters a dry type reaction device. The slaked lime powder and the activated carbon powder are sprayed into a Venturi flue in front of a bag type dust collector to further remove acidic substances in the flue gas and adsorb most harmful substances such as dioxin and the like.

The bag-type dust remover removes dust with a particle size of more than 0.05um and a dust removal rate of more than 99%. The flue gas enters a spray tower and an absorption tower after passing through a bag-type dust collector and a draught fan, secondary washing absorption is adopted, the removal efficiency of acidic substances in the flue gas is ensured, and the flue gas is washed to remove acidic gases such as hydrogen chloride and sulfur dioxide. And the wastewater from the washing tower enters an adjusting tank after being precipitated, and is pumped into the washing tower after the pH value is adjusted for recycling. The temperature of a smoke outlet is about 40 ℃, then the smoke is discharged at high pressure through a chimney, the chimney is provided with a lightning rod, smoke on-line detection and the like, and the smoke in-situ oxidation system is used for ensuring that the treatment discharge of the belt type in-situ oxidation whole system meets the environmental protection requirement.

EXAMPLE six

The disposal object of the in-situ oxidation hazardous waste disposal system in the embodiment is waste salt with the water content of more than 25%.

The method of the fifth embodiment is adopted for processing in the present embodiment. Wherein, the pretreatment system firstly uses a roller dryer or a paddle dryer or a centrifugal type to dewater before pelleting, reduces the water content in the waste salt to below 15 percent, and then adds adhesive or a proper proportion of water for pelleting.

EXAMPLE seven

The treatment object of the in-situ oxidation hazardous waste treatment system is chlor-alkali industrial waste salt with the particle size of 0.5 mm-2 mm. Wherein the TOC is not more than 2000 PPm. Wherein, the pretreatment: the bran shells and the biomass carbon powder are added into waste salt according to a certain proportion, and are directly conveyed to a distributing device for spreading after being uniformly stirred by a double-helix stirring machine. The bottom of the skip car uses a fixed detachable high-temperature-resistant mesh plate, and a high-temperature-resistant filter element ball is used between the mesh plate and the grate. The drying, preheating, roasting and cooling processes all adopt the corresponding process method of the fifth embodiment.

Example eight

In this embodiment, the disposal object of the in-situ oxidation hazardous waste disposal system is chlorine alkali industrial waste salt with TOC of 8000PPm or less, and after the belt-type in-situ oxidation, the TOC measured is 8PPm or less.

Example nine

The disposal object of the in-situ oxidation hazardous waste disposal system is waste salt with TOC 20000-100000, and the disposal is performed by the method of the fifth embodiment. Wherein, the pretreatment: mixing waste salt with TOC 20000-100000 and waste salt including but not limited to about 10: 1-10 in weight ratio, and granulating. And (4) sending the pretreated and granulated waste salt into a belt type in-situ oxidation device, and treating according to the method of the fifth embodiment.

Example ten

The treatment object of the in-situ oxidation hazardous waste treatment system is domestic sludge. Wherein, the pretreatment system: a. plate-frame filter pressing, stacked-screw sludge dewatering, dewatering and drying by a paddle dryer and a roller dryer, and then granulating and sending into a belt type in-situ oxidation device for high-temperature oxidation treatment. b. Lime and polyaluminium chloride are mixed with domestic sludge according to a certain proportion, the mixture is subjected to filter pressing and dehydration, and then a proper amount of bran shells and straw biomass fuel are added to prepare mixed sludge which is sent to a belt type in-situ oxidation device for high-temperature oxidation. Wherein, the drying, preheating, oxidizing, cooling and thermal decomposing system and the tail gas purifying and processing system all adopt the method of the fifth embodiment.

EXAMPLE eleven

The disposal object of the in-situ oxidation hazardous waste disposal system is oily sludge.

The water content of the oily sludge is more than 30-80 percent, and the oily sludge generally comprises oil-in-water, water-in-oil and suspended solids. The oily sludge contains heavy metals such as copper, chromium, mercury and the like, harmful microorganisms, organic pollutants mainly comprising polychlorinated biphenyl, phenol, benzene and the like, and water in the oily sludge contains free water, interstitial water, attached water and chemically combined water. Wherein the interstitial water accounts for 70 percent, the capillary water accounts for 20 percent, and the absorbed water accounts for 10 percent. The pretreatment is said to be dehydration first.

Example twelve

Firstly, quenching and tempering. Concentration, chemical conditioning (CP tempering) and dehydration. Through the steps of tempering and mechanical separation, the oil-water-sludge three-phase separation of the oil-containing sludge is realized. Adding inorganic flocculating agents PAC, organic flocculating agents PAM, coagulant aids CaO, surfactants, demulsifiers, pH regulators and the like in different proportions according to the properties of the oil sludge, then dehydrating by using a membrane filter press until the water content is reduced to below 30%, adding straws, bran shells and biomass fuel, mixing and feeding the mixture into a belt type in-situ oxidation system for treatment.

And (9) hardening and tempering. According to the property of the oil sludge, modifying agents with different proportions, such as ferric chloride, lime, biomass fuel, straws, bran shells and the like, are added into the oil sludge, and the mixture is mixed, mechanically pressed and dehydrated, and finally sent into a belt type in-situ oxidation system for treatment. And the in-situ oxidation treatment after the pretreatment comprises a flue gas circulating system and a tail gas treatment system which are dried, preheated, oxidized and cooled in the fifth embodiment. In the oil sludge belt type in-situ oxidation treatment process, an oil-water collection process and an oil-gas separation process and device are needed to be added, so that the oil is recycled.

Thirteen examples

The disposal object of the in-situ oxidation hazardous waste disposal system is waste incineration fly ash.

The procedure of example five was used for the treatment. Wherein, the fly ash is pretreated. And (3) chemical treatment, namely mixing and stirring the fly ash and the chemical agent by water to pulp, and converting heavy metals in the fly ash into substances with lower solubility and low toxicity. The fly ash can be leached by water, harmful heavy metals such as Cd, Pb, Cu, Zn, Cr and the like with high concentration and salts, and in the second step, a sulfuric acid solution is added to the sludge to separate out the metals and salts to the maximum extent. The saline water solution can be refined by evaporation and crystallization. The fly ash subjected to chemical pretreatment is made into particles with the particle size of 5-20 mm, the particles are sent to belt type in-situ oxidation to be subjected to high-temperature oxidation, heavy metal pollutants are effectively fixed, dioxin pollutants are thoroughly decomposed and destroyed, and the product has the characteristics of high-strength lightweight aggregate through high-temperature oxidation and can be used for casting common concrete and paving roadbed cushions. The fly ash subjected to chemical treatment is matched with coke powder to prepare particles with the particle size of 5-20 mm, and the particles are sent to belt type in-situ oxidation. The ignition temperature is normally set above 900 deg.C, the burning temperature can reach 1300 deg.C at most, and the fly ash is melted. The addition of coke powder reduces energy consumption. The melted glass state fixes heavy metals in the glass, and the leaching rate is extremely low.

Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; although the present invention has been described in detail with reference to the foregoing embodiments, it should be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; such modifications and substitutions do not depart from the spirit and scope of the present invention.

Claims

1. An in-situ oxidation hazardous waste disposal system, comprising: a pretreatment mixing granulation system, a belt type in-situ oxidation device, a flue gas circulation system and a tail gas treatment system;

the pretreatment mixing granulation system is connected with the belt type in-situ oxidation device;

a skip (15) of the belt type in-situ oxidation device sequentially passes through a drying section (13), a preheating section (12), an oxidation section (11) and a cooling section (10) of the flue gas circulating system;

the flue gas circulation system is connected with the tail gas treatment system.

2. The in-situ oxidation hazardous waste disposal system of claim 1,

the exhaust gas treatment system comprises: a secondary combustion chamber (101), a semi-dry quenching tower (102), a Venturi reactor (103), a bag-type dust collector (104), a fan (105), a spray tower (106), an absorption tower (107), a chimney (108), an atomization device (109), an alkali liquor delivery pump (110), a clean water tank (111), a circulating tank (112), a spray pump (113), a Roots fan (114) and a star-shaped discharger (115);

the oxidation chamber (8) of the flue gas circulating system is connected with the second combustion chamber (101);

the secondary combustion chamber (101), the semi-dry quenching tower (102), the Venturi reactor (103), the bag-type dust remover (104), the fan (105), the spray tower (106), the absorption tower (107) and the chimney (108) are sequentially connected; the Roots blower (114) and the Venturi reactor (103) are both connected with the Venturi reactor (103); the clean water tank (111) is connected with the semi-dry quenching tower (102) through an alkali liquor conveying pump (110) and an atomization device (109) in sequence; the circulating tank (112) is connected with the spray tower (106) through a spray pump (113).

3. The in-situ oxidation hazardous waste disposal system of claim 1,

the pretreatment mixing granulation system comprises: the device comprises a dehydration part (37), a mixing part (38), a granulation part (39), a screening part (40), a finished product bin part (41) and a belt type in-situ oxidation device which are sequentially arranged along the material conveying direction; the dehydration part (37) is connected with the mixing part (38); the mixing part (38) is connected with the granulating part (39); the granulation part (39) is connected with the screening part (40); the screening part (40) is respectively connected with the mixing part (38) and the finished product bin part (41); and the finished product bin part (41) is connected with the belt type in-situ oxidation device.

4. The in-situ oxidation hazardous waste disposal system of claim 3,

the dewatering section (37) comprises: the device comprises a forklift feeder (63), a first raw material bin (42), a first belt scale (43), a first conveyor (44), a crusher (45), a dehydrator (46) and a second conveyor (47) which are arranged in sequence; the forklift feeder (63) is used for feeding materials into an inlet of the raw material bin (42); a first belt scale (43) is arranged below the outlet of the raw material bin (42); the output end of the first belt scale (43) is provided with a first conveyor (44); the output end of the first conveyor (44) is connected with the inlet of a crusher (45); the lower part of the outlet of the crusher (45) is connected with the inlet of the dehydrator (46); a second conveyor (47) is arranged below the outlet of the dewatering machine (46);

the mixing section (38) includes: a second raw material bin (48), a third raw material bin (49), a second belt scale (50), a stirrer (51) and a third conveyor (52) which are arranged in sequence; the output end of the second conveyor (47) is respectively connected with the inlet of the second raw material bin (48) and the inlet of the third raw material bin (49); a second belt scale (50) is arranged below the outlet of the second raw material bin (48); a second belt scale (50) is arranged below the outlet of the third raw material bin (49); the output end of the second belt scale (50) is connected with the inlet of the stirrer (51); a third conveyor (52) is arranged below the outlet of the stirrer (51);

the granulation section (39) comprises: a disc feeder (53), a granulator (54) and a fourth conveyor (55); the output end of the third conveyor (52) is connected with the inlet of the disc feeder (53); a granulator (54) is arranged below the outlet of the disc feeder (53); a fourth conveyor (55) is arranged below the outlet of the granulator (54);

the screening section (40) comprises: a screening machine (56), a drying machine (57), a fifth conveyor (58) and a sixth conveyor (59); the output end of the fourth conveyor (55) is connected with the inlet of the screening machine (56); the dryer (57) is arranged below the first outlet of the screening machine (56); a fifth conveyor (58) is arranged below the second outlet of the screening machine (56); the output end of the fifth conveyor (58) is connected with the inlet of the stirrer (51); a sixth conveyor (59) is arranged below the outlet of the dryer (57);

the finished product bin portion (41) comprises: a first finished product bin (60), a second finished product bin (61) and a seventh conveyor (62); the output end of the sixth conveyor (59) is respectively connected with the inlet of the first finished product bin (60) and the inlet of the second finished product bin (61); a seventh conveyor (62) is arranged below the outlet of the first finished product bin (60); a seventh conveyor (62) is arranged below the outlet of the second finished product bin (61); the output end of the seventh conveyor (62) is connected with the inlet of a distributing device (14) of the belt type in-situ oxidation device.

5. The in situ oxidation hazardous waste disposal system of claim 1, wherein said flue gas recirculation system comprises: an oxidation chamber (8), a drying section (13), a preheating section (12), an oxidation section (11) and a cooling section (10); the drying section (13), the preheating section (12), the oxidation section (11) and the cooling section (10) are sequentially arranged along the feeding direction; the outlet of the oxidation chamber (8) is connected with the upper end of an oxidation section (11) through a first heat exchanger (9) by an oxidation section air supply pipe (1); the lower end of the oxidation section (11) is connected with the upper end of the preheating section (12) through an oxidation section exhaust pipe (2) by a first fan (27); the lower end of the preheating section (12) is connected with the upper end of the drying section (13) through a second fan (28) by a preheating section exhaust pipe (3); the lower end of the drying section (13) is connected with an inlet of the oxidation chamber (8) through a drying section exhaust pipe (4) via a third fan (29), a desulfurizer (6), a dust remover (33) and a second heat exchanger (7); the upper end of the cooling section (10) is connected with the lower end of the cooling section (10) through a cooling section circulating air pipe (5) via a second heat exchanger (7) and a fourth fan (30).

6. The in situ oxidation hazardous waste disposal system of claim 5,

the upper end of the oxidation chamber (8) is provided with a first outlet and a second outlet;

the lower end of the oxidation chamber (8) is provided with an inlet;

the oxidation chamber (8) is sequentially provided with a first ignition device and a second ignition device from bottom to top;

the first ignition device is used for carrying out first combustion on the flue gas input from the inlet of the oxidation chamber (8); the second ignition device is used for carrying out secondary combustion on the flue gas input from the inlet of the oxidation chamber (8).

7. The in-situ oxidation hazardous waste disposal system according to claim 5, wherein the first heat exchanger (9) is connected with a first outlet of the oxidation chamber (8), and the flue gas in the oxidation section air feeding pipe (1) is cooled after passing through the first heat exchanger (9).

8. The in-situ oxidation hazardous waste disposal system according to claim 5, wherein the second heat exchanger (7) has a first heat exchange channel and a second heat exchange channel; the flue gas in the first heat exchange channel and the flue gas in the second heat exchange channel have a heat exchange effect; the flue gas in the exhaust pipe (4) of the drying section passes through the first heat exchange channel to realize temperature rise; and the flue gas in the cooling section circulating gas pipe (5) is cooled through a second heat exchange channel.

9. The in-situ oxidation hazardous waste disposal system of claim 1, wherein said belt-type in-situ oxidation device comprises: the device comprises a distributing device (14), a vertical guide rail, a plurality of material trucks (15), a head star wheel (16), a tail star wheel (17) and a smoke circulating system; the head star wheel (16) is arranged at the head part of the vertical guide rail; the tail star wheel (17) is arranged at the tail part of the vertical guide rail; the vertical guide rail is provided with a plurality of movable skip cars (15), and the skip cars (15) are connected end to end; the skip car (15) is connected with the head star wheel (16) when passing through the head of the vertical guide rail, and moves from the lower layer to the upper layer of the vertical guide rail under the drive of the head star wheel (16); the skip car (15) is connected with the tail star wheel (17) when passing through the tail part of the vertical guide rail and moves from the upper layer to the lower layer of the vertical guide rail under the drive of the tail star wheel (17); the upper layer of the vertical guide rail sequentially passes through a drying section (13), a preheating section (12), an oxidation section (11) and a cooling section (10) of a flue gas circulating system; the distributing device (14) is positioned in front of the drying section (13) and above the vertical guide rail.

10. The in-situ oxidation-hazardous waste disposal system according to claim 9, wherein a material recovery bin (26) is provided below the distributing device (14).