CN116731739A - Method for simultaneously treating waste plastics and waste active adsorption material - Google Patents

Abstract

The present invention relates to the technical field of solid pollutant treatment and resource utilization, and specifically, to a method for simultaneously treating waste plastics and waste active adsorption materials. The treatment method includes: thermally dissolving waste plastics and oil, removing corrosive gases to form a dissolved liquid; and then subjecting the dissolved liquid to a catalytic reaction to form an olefin-rich gas product, an aromatic-rich liquid product and a high-concentration liquid. coke catalyst, while desorbing the waste activated carbon adsorbed with VOCs to recover VOCs resources; then, the high coke catalyst is coked with waste active adsorption materials, wherein the waste active adsorption materials include waste activated carbon and/or waste activated coke . This processing method not only solves the problem of difficulty in processing waste activated carbon and/or waste activated coke, but also solves the problem of device heat balance due to low coke generation and insufficient heat from waste plastic cracking.

Description

Method for simultaneously treating waste plastics and waste active adsorption materials

Technical Field

The invention relates to the technical field of solid pollutant treatment and resource utilization, and in particular to a method for simultaneously treating waste plastics and waste active adsorption materials.

Background Art

Plastic pollution is also known as white pollution. White pollution is a vivid name for the phenomenon of waste plastics polluting the environment. It refers to plastic products such as packaging bags, agricultural mulch, disposable tableware, plastic bottles and sealing materials made of polymer compounds such as polyethylene (PE), polypropylene (PP), polystyrene (PS), polyvinyl chloride (PVC), acrylonitrile-butadiene-styrene copolymer (ABS), polyethylene terephthalate (PET) and polytetrafluoroethylene (PTFE), which are discarded as solid waste after use. Due to random littering and difficulty in degradation, they cause pollution to the ecological environment and landscape.

At present, most methods for treating waste plastics are landfill, incineration or pyrolysis. Waste plastics are generally not easy to degrade, and the degradation cycle after landfill is hundreds of years. Landfilling cannot fundamentally solve the problem of white pollution of waste plastics. When burning waste plastics, the incineration temperature is above 1000°C, which is easy to produce thermal NOx secondary pollutants. If the waste plastics contain aromatic hydrocarbons and halogenated aromatic hydrocarbons, it is easy to produce polycyclic aromatic hydrocarbons, dioxins and other carcinogens when burned at high temperatures. For example, CN115975660A discloses a thermally self-sustaining waste plastic cascade pyrolysis coupled pyrolysis oil and gas catalytic upgrading device and method, which achieves energy saving and cracking oil quality improvement through energy cascade optimization and process optimization of the pyrolysis process. CN116064069A discloses a method for preparing fuel oil from waste plastics, and finally obtains a fuel oil product through pyrolysis reaction, product separation, product refining and other processes. However, the above-mentioned simple pyrolysis treatment of waste plastics has problems such as high energy consumption, complex pyrolysis equipment and poor oil quality.

It is generally difficult to pyrolyze PVC, ABS and PTFE by pyrolysis of waste plastics. The components such as HCl, HF and _NH3 produced during the thermal cracking or catalytic cracking/decomposition process seriously corrode the equipment in the cracking reaction system. They also react with _NH3 to generate crystals of ammonium chloride and other salts, which block the equipment pipelines and cause under-scale corrosion, seriously affecting the safe operation and long-term production of the production equipment.

On the other hand, the adsorption of low-concentration, non-continuous VOCs waste gas by granular activated carbon is a commonly used method in the industry to reduce the concentration of VOCs waste gas and achieve standard emission of VOCs waste gas. After multiple regenerations, the activated carbon/activated coke adsorbent adsorbed with VOCs fails due to the destruction of the microporous structure, loses its adsorption activity, and becomes waste activated carbon. Some waste activated carbon has become hazardous waste because it contains malignant and harmful components. At the same time, activated carbon adsorption is widely used in wastewater purification. After multiple adsorption and regeneration, the activated carbon is also deactivated and finally becomes hazardous waste.

Waste activated carbon is generally treated by incineration and rotary kiln regeneration. For example, CN115945183A discloses a method for regenerating waste activated carbon, which uses a moving bed regeneration method to integrate the preheating section, regeneration section and cooling section into a single device. The waste activated carbon undergoes three steps of preheating, regeneration and cooling to complete the regeneration, thereby reducing the wear rate of the activated carbon. However, existing activated carbon regeneration devices all have problems such as high energy consumption, small processing capacity, low regeneration temperature, incomplete regeneration, and poor regeneration effect.

Therefore, it is urgent to develop a method for treating waste plastics and waste activated carbon/waste activated coke that is inherently safe and comprehensively utilized as resources, so as to turn waste into treasure. In view of this, the present invention is proposed.

Summary of the invention

The purpose of the present invention is to provide a method for simultaneously treating waste plastics and waste activated adsorbent materials. The treatment method provided by the embodiment of the present invention can simultaneously recycle waste plastics and waste activated carbon or waste activated coke and other waste activated adsorbent materials, on the one hand, catalytically cracking or catalytically pyrolyzing waste plastics into valuable petrochemical products, on the other hand, converting waste activated carbon or waste activated coke into high-grade energy, and providing the heat required for the catalytic cracking/pyrolysis of waste plastics, integrating the harmless treatment of waste activated carbon and/or waste activated coke into the catalytic pyrolysis process of waste plastics.

The present invention is achieved in that:

In a first aspect, an embodiment of the present invention provides a method for simultaneously treating waste plastics and waste activated adsorption materials, comprising: thermally dissolving waste plastics and oil to form a dissolved liquid after removing corrosive gases; then subjecting the dissolved liquid to a catalytic reaction to form an olefin-rich gas product, an aromatics-rich liquid product and a high-coke catalyst, and simultaneously desorbing waste activated carbon adsorbed with VOCs to recover VOCs resources; then, charring the high-coke catalyst and the waste activated adsorption material, wherein the waste activated adsorption material comprises waste activated carbon and/or waste activated coke.

In a preferred embodiment, waste plastics are mixed with oil and thermally dissolved at a temperature of 180-310°C and a pressure of normal pressure-0.3MPa(g). During the thermal dissolution process, an inert stripping gas is introduced to remove corrosive gases. The corrosive gases from the stripping gas are removed from the harmful non-metal removal system to solve the effect of corrosive components on the long-term operation of the equipment of the catalytic cracking/decomposition unit.

The oil includes any one of catalytic cracking feedstock oil, catalytic cracking feedstock oil, light diesel oil, heavy cycle oil and oil slurry, or a mixture of at least two of them; the corrosive gas includes, but is not limited to, HCl, HF and NH _3. The inert gas is a gas that does not contain O ₂ ; for example, it includes, but is not limited to, any one of N ₂ , CO ₂ , natural gas and refinery gas, or a mixture of at least two of them.

Furthermore, the inert gas flow rate is controlled so that the empty tower linear velocity through the thermal dissolution container is 0.1-2.0 m/s. Meanwhile, the stirring speed of the thermal dissolution is 1-500 rpm. The mass ratio of the waste plastic to the oil is 00.1-0.5:1.

In a preferred embodiment, the dissolved liquid from which the corrosive gas is removed is subjected to a catalytic reaction, specifically by pumping the dissolved liquid into a catalytic reaction unit for a catalytic reaction.

At the same time, the waste active adsorption material also enters the catalytic reaction unit for catalytic reaction, and is specifically injected into the catalytic reactor of the catalytic reaction unit through a feeder (such as a screw feeder, a fluidized feeder, etc.) for catalytic reaction. The waste active adsorption material is selected from waste activated carbon and/or waste activated coke. The mass ratio of waste plastic to the waste active adsorption material is 1:0.01-0.2.

The VOCs components adsorbed in the waste activated carbon and/or waste activated coke are desorbed by high temperature (e.g. 470-580°C) and steam stripping, and recovered with the catalytic reaction products. Specifically, the products formed by the catalytic reaction include olefin-rich gas products, aromatic-rich liquid products and high-coke catalysts. That is to say, the gas and liquid products produced by the catalytic reaction unit enter the product separation system together to recover olefins, aromatics, oil products and other petrochemical products.

In a preferred embodiment, the catalyst used in the catalytic reaction is a low-coke catalyst, which can be a commercially available catalyst or a regenerated catalyst formed by burning a high-coke catalyst in an embodiment of the present invention. The high-coke catalyst is a product of solid coke attached to the surface of the low-coke catalyst formed by the catalytic reaction.

In a preferred embodiment, the carbon content of the low coke catalyst is 0.01-0.35wt%, and the carbon content of the high coke catalyst is 0.5-1.5wt%.

In a preferred embodiment, the high-coke catalyst and the waste activated adsorption material that has completed VOCs desorption through the catalytic reaction are charred. Specifically, the high-coke catalyst produced after the catalytic reaction flows into the charcoal burning unit by gravity difference, and enters the charcoal burning unit with the waste activated carbon and/or waste activated coke it carries to realize the co-combustion of the waste activated carbon/coke and the high-coke catalyst, and at the same time realize the regeneration of the high-coke catalyst. The flue gas produced by the combustion enters the subsequent flue gas energy recovery system and flue gas purification system of the charcoal burning unit by its own pressure, and finally achieves the standard emission of flue gas.

The high-coke catalyst (regenerated catalyst) is converted into a low-coke catalyst (regenerated catalyst) during the coke burning unit process, and the low-coke catalyst flows into the above-mentioned catalytic reaction unit under a fluidized state by pressure difference.

Specifically, the heat released by the combustion of waste activated adsorption materials such as waste activated carbon and/or waste activated coke is absorbed by the high-coke catalyst and circulated back to the catalytic reaction unit for use in the cracking reaction of the hot liquid in the catalytic reaction unit, which not only solves the problem of difficult treatment of waste activated carbon and/or waste activated coke, but also solves the thermal balance problem of the device with low coke yield and insufficient heat in the cracking of waste plastics.

Furthermore, the charring conditions include: a temperature of 590-750° C. and a pressure of 0.1-0.3 MPa(g).

The present invention has the following beneficial effects: On the one hand, the treatment method provided by the embodiment of the present invention uses waste plastics as a blending component of the raw materials for catalytic reaction, and converts them into low-carbon olefins such as ethylene and propylene and petrochemical products such as oil products during the catalytic reaction process. The waste activated carbon and/or waste activated coke adsorbed with VOCs are added to the catalytic reaction unit to recover the organic compound components in the waste activated carbon and/or waste activated coke. At the same time, HCl, HF and _NH3 are stripped out through the dissolution and impurity removal unit for treatment, thereby solving the effect of corrosive components on the long-term operation of the equipment of the catalytic cracking/decomposition device. On the other hand, waste activated carbon and/or waste activated coke are used as charring heat source components, and the combustion heat is converted into high-grade energy, thereby reducing the energy consumption of the petroleum catalytic cracking/decomposition device due to the catalytic cracking/decomposition of waste plastics, and even reducing the energy consumption of the catalytic cracking/decomposition device instead of increasing it.

BRIEF DESCRIPTION OF THE DRAWINGS

In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings required for use in the embodiments are briefly introduced below. It should be understood that the following drawings only show certain embodiments of the present invention and therefore should not be regarded as limiting the scope. For ordinary technicians in this field, other related drawings can be obtained based on these drawings without creative work.

FIG. 1 is a device for implementing a method for simultaneously treating waste plastics and waste active adsorption materials provided by an embodiment of the present invention.

Diagram: 1-hot dissolution tank; 2-feed pump; 3-activated carbon feeder; 4-rising tube reactor; 5-stripper; 6-settler; 7-coke burner; 8-waiting inclined tube; 9-regeneration inclined tube.

DETAILED DESCRIPTION

In order to make the purpose, technical scheme and advantages of the embodiments of the present invention clearer, the technical scheme in the embodiments of the present invention will be described clearly and completely below. If the specific conditions are not specified in the embodiments, they are carried out according to conventional conditions or conditions recommended by the manufacturer. If the manufacturer of the reagents or instruments used is not specified, they are all conventional products that can be purchased commercially.

The embodiment of the present invention provides a method for simultaneously treating waste plastics and waste active adsorption materials, comprising:

Waste plastics are sent into the hot dissolution tank in an inert gas atmosphere and are thermally dissolved with oil at a temperature of 180-310°C under stirring; corrosive gases such as HCl, HF and _NH3 generated during the dissolution process are stripped out by the inert gas entering from the bottom of the hot dissolution tank and sent to the corrosive gas treatment system.

The insoluble impurity components contained in the waste plastics are discharged from the dissolution and impurity removal unit system from the slag discharge port at the bottom of the hot dissolution tank. The dissolution liquid produced after the waste plastics and oil products are thermally dissolved is fed from the middle and lower outlet of the hot dissolution tank through a feed pump to the lower inlet of the riser reactor of the catalytic reaction unit, and contacts with the high-temperature (590-750°C) low-coke catalyst (regenerated catalyst) from the coke burner, goes up along the riser reactor and undergoes catalytic cracking/decomposition reaction, and then enters the settler at the top of the catalytic reaction unit to separate the catalyst from the reaction product.

Waste activated carbon and/or waste activated coke is fed into the settler at the top of the catalytic reaction unit through a feeder in an inert gas atmosphere, and mixed with the catalyst, reactants and products at a temperature between 470 and 580° C. from the outlet of the reverse riser reactor.

After the reaction is completed, the high-coke catalyst (recycled catalyst) and solid particles such as waste activated carbon and/or waste activated coke are moved downward by gravity to the stripper of the catalytic reaction unit in the settler. The entrained and adsorbed oil and gas including VOCs are stripped out by the steam from the bottom of the stripper and leave the settler together with the reaction products to the product separation system to recover petrochemical products such as olefins, aromatics and oil products.

After the high-coke catalyst (catalyst to be regenerated) and waste activated carbon and/or waste activated coke are stripped to remove oil and gas (including VOCs), they flow into the coke burner (catalyst regenerator) through the inclined tube to be regenerated, and burn at high temperature (590-750℃) with the air from the bottom of the coke burner in a fluidized state. The generated flue gas is treated by the flue gas energy recovery and purification system and then discharged.

Waste activated carbon and/or waste activated coke reacts with air in a coke burner to generate flue gas and trace dust, which are discharged along with the combustion flue gas; high-coke catalyst (catalyst to be generated) is converted into low-coke catalyst (regenerated catalyst) after passing through the coke burner, and then circulates back to the bottom of the riser reactor through the regeneration inclined tube to continue reacting with the dissolved liquid of waste plastics and oil products.

The heat released by the combustion of waste activated carbon and/or waste activated coke in the coke burner is absorbed by the catalytic cracking/decomposition catalyst and circulated back to the riser reactor for the mixed catalytic reaction of the raw oil and waste plastics in the catalytic reaction unit. The method of the present invention not only solves the problem of difficult treatment of waste activated carbon/coke, but also solves the problem of heat balance of the device with low coke production and insufficient heat in the cracking of waste plastics.

The features and performance of the present invention are further described in detail below in conjunction with the embodiments.

The waste plastics used in the following examples and comparative examples are GDG-05 waste plastic particles purchased from the market, and their physicochemical properties are shown in Table 1; the waste activated carbon used in the examples and comparative examples are waste activated carbon samples CC-01 and MC-02 collected from R Coating Company and Z Machinery Factory, and their physicochemical properties are shown in Table 2. The oil used in the examples and comparative examples is heavy oil and catalytic oil slurry taken from Ningxia Yinshan Energy Chemical Co., Ltd., and its physicochemical properties are shown in Table 3. The catalyst used in the examples and comparative examples is a heavy oil catalytic cracking equilibrium catalyst taken from Ningxia Yinshan Energy Chemical Co., Ltd., and its physicochemical properties are shown in Table 4.

Table 1 Composition and properties of waste plastics

*Ash is primarily calcium carbonate, a filler component in plastic products.

Table 2 Composition and properties of waste activated carbon

*The composition of VOCs is toluene 75%wt and n-butanol 25%wt.

Table 3 Physicochemical properties of heavy oil

Table 4 Catalytic cracking catalyst properties

Example 1

This embodiment provides a method for simultaneously performing thermal melt treatment on waste plastics, comprising:

Thermal dissolution and dechlorination of waste plastics and heavy oil. 160 kg of heavy oil was added to a 300-liter hot oil-heated enamel dissolving tank with a water vapor inlet at the bottom, a 90°C hot water condensation reflux outlet at the top, and an agitator inside. The tank was heated while stirring at a stirring speed of 120 rpm and a heating rate of 5°C/min. When the temperature rose to 190°C, 40 kg of waste plastic GDC-05 was added to the dissolving tank at a rate of 10 kg/min. At the same time, stirring and heating were continued. When the temperature rose to 215°C, the completely dissolved dissolved liquid was sampled and analyzed, and then the water vapor inlet valve at the bottom of the dissolving tank and the circulating condensate valve of the reflux device at the top of the dissolving tank were opened. Saturated water vapor of 0.35 MPa (g) entered the dissolved liquid from the bottom of the dissolving tank at a rate of 5 liters/min. The dissolved liquid continued to be stirred and heated in the dissolving tank and steam stripped until the temperature reached 320°C. The temperature was stopped and steam stripping continued for 10 minutes to obtain a purified mixed dissolved liquid in the dissolving tank. Aqueous hydrogen chloride solution (dilute hydrochloric acid) is obtained at the top outlet of the dissolving tank. After dissolving and dechlorinating, the dechlorinated solution is sampled and analyzed. The analysis results are shown in Table 5.

Table 5 Elemental composition of waste plastics and heavy oil solution before and after dechlorination

Sample name C*, wt% H, wt% S, wt% N, wt% Cl, wt% Dissolved liquid before dechlorination 84.29 12.06 0.54 0.24 0.23 Dechlorinated solution 84.66 12.11 0.54 0.26 0.001

*Excluding carbon from calcium carbonate.

It can be seen from the experimental results and the analytical data in Table 5 that the waste plastic GDC-05 and the heavy oil in Table 3 can be completely dissolved into a uniform fluid liquid material at a temperature of 190-220°C in 20 minutes. During the slow heating process of 220°C-320°C, the PVC waste plastic component contained in the liquid material can be completely decomposed into HCl, and the chlorine removal rate of the mixed liquid is 99.57%, which greatly alleviates the corrosion of elemental chlorine to processing equipment in subsequent processing.

Example 2

The embodiment of the present invention provides a method for simultaneously treating waste plastics and waste active adsorption materials, comprising: pumping a dissolving liquid into the lower inlet of a riser reactor of a catalytic reaction unit, contacting with a catalyst, ascending along the riser reactor and undergoing a catalytic cracking/decomposition reaction. At the same time, waste activated carbon is fed into a settler at the top of the catalytic reaction unit through a feeder in an inert gas atmosphere, and mixed with the catalyst, reactants and products from the outlet of the reverse riser reactor.

After the reaction is completed, the high-coke catalyst (recycled catalyst) and waste activated carbon are moved down to the stripper of the catalytic reaction unit by gravity in the settler. The entrained and adsorbed oil and gas including VOCs are stripped out by the steam from the bottom of the stripper and leave the settler together with the reaction products to the product separation system to recover olefins, aromatics, oil products and other petrochemical products.

After the high-coke catalyst (catalyst to be regenerated) and waste activated carbon are stripped to remove oil and gas (including VOCs), they flow into the coke burner (catalyst regenerator) through the inclined tube to be regenerated, and burn at high temperature with the air from the bottom of the coke burner in a fluidized state. The generated flue gas is treated by the flue gas energy recovery and purification system and then discharged.

The method uses the CGP-1 equilibrium catalyst shown in Table 4, the dechlorination solution obtained in Example 1, and the waste activated carbon CC-01 shown in Table 2. The amount of waste activated carbon added is 50 g/h, and other process operating conditions are shown in Table 6. The experimental results are shown in Table 7.

Example 3

The treatment method provided in Example 3 is identical to the treatment method provided in Example 2, except that the amount of waste activated carbon added is 200 g/h. The process operating conditions are shown in Table 6, and the experimental results are shown in Table 7.

Comparative Example 1

The treatment method provided in Comparative Example 1 is compared with the treatment method provided in Example 2, except that the feed of the device is changed to heavy oil (properties are shown in Table 3), and other conditions are exactly the same, and the process operating conditions are shown in Table 6. The experimental results are shown in Table 7.

Comparative Example 2

The treatment method provided in Comparative Example 2 is compared with the treatment method provided in Comparative Example 1, except that the amount of waste activated carbon added is 200 g/h, and other conditions are exactly the same. The process operating conditions are shown in Table 6. The experimental results are shown in Table 7.

Comparative Example 3

Comparative Example 3 is a control experiment using heavy oil (properties shown in Table 3) as feedstock and without adding waste activated carbon, which is equivalent to a typical heavy oil catalytic cracking experiment, and the process operating conditions are shown in Table 6. The experimental results are shown in Table 7.

Table 6 Main operating conditions of the experimental device

Table 7 Comparison of experimental results

Comparing the experimental conditions in Table 6 with the experimental results in Table 7, it can be seen that:

1. Compared with pure heavy oil (Comparative Examples 1-3), the yield of low-carbon olefins (ethylene+propylene+butene) obtained by catalytic cracking of a mixed liquid of 20% waste plastic GDC-05 and 80% heavy oil (Example 2 and Example 3) can be increased from 15.16wt% to 20.42wt%, an increase of 34.70%. In addition to low-carbon olefins, the cracking of waste plastics also produces a part of light alkanes and gasoline rich in aromatics (BTEX). It shows that the process provided by the present invention can effectively convert waste plastics into petrochemical raw materials such as low-carbon olefins, light aromatics and oil products. In this process, the cracking of waste plastics does not produce hydrogen and methane, and the coke rate is much lower than that of heavy oil raw materials. It is an ideal and effective way to treat waste plastics.

2. Waste activated carbon and a mixed liquid of 20% waste plastic GDC-05 and 80% heavy oil were jointly processed by the process method of the present invention (Examples 2-3 and Comparative Examples 1-2). Compared with the processing of pure heavy oil alone (Comparative Example 3), on the one hand, the VOCs resources contained in the waste activated carbon can be fully and effectively recovered, and on the other hand, the heat released by the combustion of the waste activated carbon entering the charcoal burning unit after the VOCs are removed in the reaction unit can be used for the heat required for the catalytic reaction unit to crack the waste plastic or/and heavy oil. From the power consumption indicators of the above Examples 2-3 and Comparative Examples 1-3, the effect is very obvious. The waste activated carbon added increased from 0 g/hour (Comparative Example 3) to 50 g/hour (Comparative Example 1) and then to 200 g/hour (Comparative Example 2), and the power consumption E4 of the coke burner decreased from 1854 watts to 1417 watts and then to 106 watts. The heat released by the combustion of waste activated carbon is utilized in the cracking reaction of waste plastics. This result is directly reflected in the data (E1+E2+E3-E4) of the comparison between Example 2 and Comparative Example 1, and between Example 3 and Comparative Example 2 (power consumption of coke burner - power consumption of riser reactor, catalyst settler and catalyst stripper of catalytic reaction unit).

3. The heat generated by the combustion of coke produced by the cracking of waste activated carbon and waste plastics and carried away by the flue gas, as well as the sulfur, nitrogen and solid impurities in the waste plastics and waste activated carbon can be further recovered and purified by the flue gas energy recovery and purification system, thereby realizing the technical essence of the technical route of the present invention while maintaining environmental friendliness while recycling resources.

Example 4

This embodiment provides a device for implementing the processing method (see FIG1 ), and the specific structure is as follows:

It includes a hot dissolving unit, a catalytic reaction unit and a charring unit connected in sequence. Specifically, the hot dissolving unit includes two hot dissolving tanks 1, which are arranged in parallel, the catalytic reaction unit includes a settler 6, a stripper 5 and a riser reactor 4 connected in sequence, the charring unit includes a coke burner 7, the hot dissolving tank 1 is connected to the riser reactor 4 through a feed pump 2, the catalyst outlet of the stripper 5 is connected to the high coke catalyst inlet of the coke burner 7 through a regenerated inclined pipe 8, the riser reactor 4 is connected to the low coke catalyst outlet of the coke burner 7 through a regeneration inclined pipe 9, and the activated carbon feeder 3 is connected to the settler.

In FIG. 1 , A represents oil; B represents waste plastic; C represents inert gas; D represents waste activated carbon; E represents water vapor; and F represents air.

Among them, the device shown in Figure 1 is small in scale and has a large heat dissipation capacity. In order to achieve the heat balance of the device, its heating and heat preservation all rely on electric heating. The mixed liquid processing capacity of the device (the flow rate of the feed pump 2) is 5kg/h. The inner diameter of the riser reactor 4 of its catalytic reaction unit is 16mm and the height is 3200mm, the inner diameter of the catalyst settler 6 is 160mm and the height is 800mm, and the inner diameter of the catalyst stripper 5 is 120mm and the height is 700mm. The coke burner 7 of the coke burning unit of the device has an inner diameter of 260mm and a height of 600mm in the upper dilute phase section, and an inner diameter of 100mm and a height of 650mm in the lower dense phase section. The solid activated carbon feed rate of the active feeder 3 of the device is 100-300g/h. The inner diameters of the waiting inclined tube 8 and the regeneration inclined tube 9 are both 12mm.

It should be noted that the above-mentioned device is only an example of implementing the above-mentioned method of simultaneously treating waste plastics and waste active adsorption materials, and is not limited to the above-mentioned device.

The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. For those skilled in the art, the present invention may have various modifications and variations. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention shall be included in the protection scope of the present invention.

Claims (10)

1. A method for simultaneously treating waste plastics and waste active adsorbent materials, comprising: waste plastics and oil materials are thermally dissolved, and corrosive gases are removed to form dissolved liquid;

then carrying out catalytic reaction on the dissolved liquid to form a gaseous product rich in olefin, a liquid product rich in aromatic hydrocarbon and a high coke catalyst, and simultaneously desorbing and recovering VOCs resources from the waste activated carbon adsorbed with VOCs in a catalytic reaction system;

the high coke catalyst is then burnt with a spent active adsorbent material, wherein the spent active adsorbent material comprises spent activated carbon and/or spent activated coke.

2. The method for simultaneously treating waste plastics and waste active adsorbent materials according to claim 1, wherein the oil comprises any one or a mixture of at least two of catalytic cracking raw oil, light diesel oil, heavy cycle oil and slurry oil;

the corrosive gas comprises HCl, HF and NH ₃ 。

3. The method of simultaneously treating waste plastic and waste active adsorbent material according to claim 1, wherein the conditions of thermal dissolution comprise: the temperature is 180-310 ℃, the pressure is normal pressure-0.3 MPa (g), the atmosphere is inert gas atmosphere, the stirring speed of thermal dissolution is 1-500rpm, and the superficial linear speed of inert gas is 0.1-2.0m/s;

preferably, the removed corrosive gas is transported to a harmful nonmetallic removal system for treatment.

4. The method for simultaneously treating waste plastics and waste active adsorbing material according to claim 3, wherein said inert gas is O-free ₂ Is a gas of (2);

preferably, it comprises N ₂ 、CO ₂ Any one or a mixture of at least two of natural gas and refinery gas.

5. The method for simultaneously treating waste plastics and waste active adsorbent materials according to claim 1, wherein the catalyst used in the catalytic reaction is a low coke catalyst;

preferably, the low-coke catalyst is selected from regenerated catalysts formed after the high-coke catalyst is burned;

preferably, the high coke catalyst is a product of a low coke catalyst with solid coke attached to the surface.

6. The method of simultaneously treating waste plastics and waste active adsorbent material according to claim 5, wherein said low coke catalyst has a carbon content of 0.01 to 0.35wt% and said high coke catalyst has a carbon content of 0.5 to 1.5wt%.

7. The method for simultaneously processing waste plastic and waste active adsorption material according to claim 1, wherein the waste active adsorption material is subjected to catalytic reaction to recover adsorbed VOCs components before being burnt;

preferably, the conditions of the catalytic reaction include: the temperature is 470-580 ℃.

8. The method for simultaneous processing of waste plastics and waste active adsorbent material according to claim 7, wherein the olefin-rich gaseous product and the aromatic-rich liquid product are separated to recover olefins, aromatics and oils.

9. The method of simultaneous treatment of waste plastic and waste active adsorbent material according to claim 1, wherein the mass ratio of waste plastic to oil is 00.1-0.5:1 and the mass ratio of waste plastic to waste active adsorbent material is 1:0.01-0.2.

10. The method of simultaneously treating waste plastic and waste active adsorbent material according to claim 1, wherein the conditions of scorching comprise: the temperature is 590-750 ℃ and the pressure is 0.1-0.3MPa (g).