CN220564546U - Device and system for simultaneously treating waste plastics and waste active adsorption materials - Google Patents
Device and system for simultaneously treating waste plastics and waste active adsorption materials Download PDFInfo
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Abstract
The utility model relates to the technical field of solid pollutant treatment and resource utilization, in particular to a device and a system for simultaneously treating waste plastics and waste active adsorption materials. The device comprises a thermal dissolution unit for thermally dissolving waste plastics and oil, a catalytic reaction unit for carrying out catalytic reaction on a thermal solution formed by the thermal dissolution unit, and a coke burning unit for burning, wherein the thermal dissolution unit, the catalytic reaction unit and the coke burning unit are sequentially connected. The device can simultaneously recycle waste active adsorption materials such as waste plastics, waste activated carbon or waste activated coke, etc., on one hand, waste plastics are catalytically cracked/decomposed into petrochemical products, on the other hand, VOCs adsorbed by the waste activated carbon or waste activated coke are recycled, the waste activated carbon or waste activated coke is converted into high-grade energy, heat required by reaction is provided for the waste plastics catalytic cracking or catalytic cracking, and harmless treatment of the waste activated carbon and/or waste activated coke is integrated into the waste plastics catalytic cracking process.
Description
Technical Field
The utility model relates to the technical field of solid pollutant treatment and resource utilization, in particular to a device and a system for simultaneously treating waste plastics and waste active adsorption materials.
Background
Plastic contamination, that is, white Pollution, is an image of the phenomenon of environmental Pollution of waste plastics, and means that plastic products such as packaging bags, agricultural mulching films, disposable tableware, plastic bottles, sealing materials and the like made of high molecular compounds such as Polyethylene (PE), polypropylene (PP), polystyrene (PS), polyvinyl chloride (PVC), acrylonitrile-butadiene-styrene copolymer (ABS), polyethylene terephthalate (PET), polytetrafluoroethylene (PTFE) are discarded as solid wastes after being used, and are difficult to degrade and treat due to random throwing, thus polluting ecological environment and landscape.
Current methods for treating waste plastics are mostly landfills, incineration or pyrolysis. Waste plastics are generally not easy to degrade, the degradation period after landfill is hundreds of years, and the problem of white pollution of the waste plastics cannot be essentially solved by landfill. When waste plastics are incinerated, the incineration temperature is above 1000 ℃, thermal NOx secondary pollutants are easy to generate, and if the waste plastics contain aromatic hydrocarbons and halogenated aromatic hydrocarbons, the waste plastics are combusted at high temperature, so that cancerogenic substances such as polycyclic aromatic hydrocarbons, dioxins and the like are easy to generate. For example, CN115975660a discloses a thermally self-supporting waste plastic cascade pyrolysis coupling pyrolysis oil gas catalytic upgrading device and method, and energy saving and pyrolysis oil upgrading are achieved through energy cascade optimization and process optimization in the pyrolysis process. CN116064069a discloses a method for preparing fuel oil from waste plastics, and finally obtaining a fuel oil product through the processes of pyrolysis reaction, product separation, product refining and the like. However, the simple pyrolysis treatment of waste plastics has the problems of high energy consumption, complex pyrolysis equipment, poor oil quality and the like.
Pyrolysis of waste plastics is generally difficult to achieve, and components such as HCl, HF and NH3 generated in the pyrolysis or catalytic cracking/pyrolysis process are severely corroded on equipment of a pyrolysis reaction system, and salt crystals such as ammonium chloride generated by reaction with NH3 are also caused to block equipment pipelines and corrode under scale, so that safe operation and long-period production of a production device are seriously influenced.
On the other hand, the granular activated carbon is used for adsorbing low-concentration discontinuous VOCs waste gas, which is a method commonly adopted in the industry, so as to reduce the concentration of the VOCs waste gas and realize the standard emission of the VOCs waste gas. After multiple regenerations, the activated carbon/activated coke adsorbent adsorbed with VOCs loses adsorption activity due to the failure of the microporous structure, and becomes waste activated carbon. Some waste activated carbon has become hazardous waste because of the containing of malignant harmful components. Meanwhile, the activated carbon adsorption has wide application in the aspect of wastewater purification, and after repeated adsorption and regeneration, the activated carbon is deactivated and finally becomes dangerous waste.
Waste activated carbon is generally treated by incineration and rotary kiln regeneration. For example, CN115945183a discloses a method for regenerating waste activated carbon, in which a preheating section, a regenerating section and a cooling section are integrated into a single device by adopting a moving bed regeneration mode, and the waste activated carbon is subjected to three steps of preheating, regenerating and cooling to complete regeneration, so that the wear rate of the activated carbon is reduced. However, the existing active carbon regeneration devices have the problems of high energy consumption, small treatment capacity, low regeneration temperature, incomplete regeneration, poor regeneration effect and the like.
Therefore, development of a treatment device for intrinsically safe and comprehensive resource utilization of waste plastics and waste activated carbon/waste activated coke is needed, and waste materials are changed into valuable materials.
Disclosure of Invention
The utility model provides a device and a system for simultaneously treating waste plastics and waste active adsorption materials. The device provided by the utility model can simultaneously recycle waste active adsorption materials such as waste plastics and waste activated carbon or waste activated coke, on one hand, catalytically crack/solve the waste plastics into precious petrochemical products, and on the other hand, recycle VOCs adsorbed by the waste activated carbon or waste activated coke, convert the waste activated carbon or waste activated coke into high-grade energy, provide heat required by reaction for the waste plastics catalytic cracking or catalytic cracking, and integrate the harmless treatment of the waste activated carbon and/or waste activated coke into the waste plastics catalytic cracking process.
The utility model is realized in the following way:
in a first aspect, an embodiment of the present utility model provides an apparatus for simultaneously processing waste plastics and waste active adsorption materials, including a thermal dissolution unit for thermally dissolving waste plastics and oil, a catalytic reaction unit for performing a catalytic reaction on a thermal solution formed by the thermal dissolution unit, and a coke burning unit for burning, where the thermal dissolution unit, the catalytic reaction unit, and the coke burning unit are sequentially connected.
Further, in a preferred embodiment of the present utility model, the thermal dissolution unit includes a thermal dissolution tank, which is in communication with the catalytic reaction unit through a feed pump.
Further, in a preferred embodiment of the present utility model, the number of the thermal dissolving tanks is plural, the plural thermal dissolving tanks are arranged in parallel, and each of the thermal dissolving tanks is communicated with the catalytic reaction unit through the feed pump.
Further, in a preferred embodiment of the present utility model, a stirring component is disposed in each of the thermal dissolution tanks, an inert gas inlet is disposed at the bottom of each of the thermal dissolution tanks, an etching gas outlet is disposed at the top of each of the thermal dissolution tanks, a slag discharging port is disposed at the bottom of each of the thermal dissolution tanks, an oil and waste plastic inlet is disposed at the upper part of each of the thermal dissolution tanks, and a hot solution outlet is disposed at the lower part of each of the thermal dissolution tanks.
Further, in a preferred embodiment of the present utility model, the catalytic reaction unit comprises a settler, a stripper and a riser reactor which are connected in sequence, the hot dissolution unit is communicated with a hot solution inlet of the riser reactor through a feed pump, and both the riser reactor and the stripper are communicated with the coke burning unit.
Further in a preferred embodiment of the utility model, the apparatus further comprises a spent activated carbon feeder in communication with the settler.
Further in a preferred embodiment of the utility model, the char-combusting unit comprises a char burner, the catalyst outlet of which communicates with the catalyst inlet of the riser reactor via a regeneration chute.
Further in a preferred embodiment of the utility model, the catalyst inlet of the coke burner is in communication with the catalyst outlet of the stripper via a spent chute.
Further, in a preferred embodiment of the present utility model, the bottom of the coke burner is provided with a gas inlet.
In a second aspect, the present utility model provides a system for simultaneously treating waste plastics and waste active adsorbent material comprising the apparatus for simultaneously treating waste plastics and waste active adsorbent material described above.
The beneficial effects of the utility model are as follows: the device provided by the utility model can simultaneously carry out resource utilization treatment on waste plastics, waste activated carbon and/or waste activated coke. Specifically, the device on one hand takes waste plastics as the blending component of the catalytic reaction raw material to carry out catalytic reaction in a catalytic unit, converts the waste plastics into low-carbon olefins such as ethylene, propylene and the like, petrochemical products such as oil products and the like, adds the waste activated carbon and/or waste activated coke adsorbed with VOCs into the catalytic reaction unit, can recycle organic compound components in the waste activated carbon and/or waste activated coke, and simultaneously uses a thermal dissolving unit to carry out HCl, HF and NH 3 Stripping out for treatment, and solving the influence of corrosive components on the long-period operation of the catalytic cracking or the equipment of the catalytic cracking device. On the other hand, the waste active carbon/waste active coke is used as the heat source component of the coke burning unit, and the combustion heat is converted intoThe energy of the product is high, the energy consumption which is increased to the petroleum catalytic cracking/catalytic cracking device by the catalytic cracking/catalytic cracking of the waste plastics is reduced, and even the energy consumption of the catalytic cracking/cracking device is not increased and reduced.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present utility model, the drawings that are needed in the embodiments will be briefly described below, it being understood that the following drawings only illustrate some examples of the present utility model and therefore should not be considered as limiting the scope, and other related drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
Fig. 1 is a schematic structural view of an apparatus for simultaneously treating waste plastics and waste active adsorbing materials according to embodiment 1 of the present utility model.
The marks in the figure are respectively: 1-a thermal dissolution tank; 2-a feed pump; 3-a waste activated carbon feeder; 4-riser reactor; a 5-stripper; a 6-settler; 7-coke burner; 8-waiting inclined tube; 9-regenerating inclined tube.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the embodiments of the present utility model more apparent, the technical solutions of the embodiments of the present utility model will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present utility model, and it is apparent that the described embodiments are some embodiments of the present utility model, but not all embodiments. All other embodiments, based on the embodiments of the utility model, which are apparent to those of ordinary skill in the art without inventive faculty, are intended to be within the scope of the utility model. Thus, the following detailed description of the embodiments of the utility model, as presented in the figures, is not intended to limit the scope of the utility model, as claimed, but is merely representative of selected embodiments of the utility model. All other embodiments, based on the embodiments of the utility model, which are apparent to those of ordinary skill in the art without inventive faculty, are intended to be within the scope of the utility model.
In the description of the present utility model, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings are merely for convenience in describing the present utility model and simplifying the description, and do not indicate or imply that the apparatus or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present utility model.
Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. In the description of the present utility model, the meaning of "a plurality" is two or more, unless explicitly defined otherwise.
In the present utility model, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the above terms in the present utility model can be understood by those of ordinary skill in the art according to the specific circumstances.
In the present utility model, unless expressly stated or limited otherwise, a first feature "above" or "below" a second feature may include both the first and second features being in direct contact, as well as the first and second features not being in direct contact but being in contact with each other through additional features therebetween. Moreover, a first feature being "above," "over" and "on" a second feature includes the first feature being directly above and obliquely above the second feature, or simply indicating that the first feature is higher in level than the second feature. The first feature being "under", "below" and "beneath" the second feature includes the first feature being directly under and obliquely below the second feature, or simply means that the first feature is less level than the second feature.
Example 1
The device provided by the embodiment of the utility model can process waste plastics and waste active adsorption materials at the same time, and comprises a thermal dissolving unit for thermally dissolving the waste plastics and the oil. Specifically, the thermal dissolution unit comprises 2 thermal dissolution tanks 1, wherein the 2 thermal dissolution tanks 1 are arranged in parallel, each thermal dissolution tank 1 is internally provided with a stirring component, and materials in the thermal dissolution tanks 1 are stirred and mixed. The bottom of each thermal dissolution tank 1 is provided with an inert gas inlet, so that inert gas can be introduced into the thermal dissolution tank 1 to generate HCl, HF and NH in the thermal dissolution process in the thermal dissolution tank 1 3 And stripping with an isocratic gas. Meanwhile, the top of each thermal dissolution tank 1 is provided with a corrosive gas outlet, so that the stripped corrosive gas is sent to a subsequent corrosive gas treatment system.
Further, the upper part of each thermal dissolving tank 1 is provided with an oil and waste plastic inlet, and then waste plastic and oil are introduced into the thermal dissolving tank 1, so that the waste plastic and the oil can be thermally dissolved in the thermal dissolving tank 1. The bottom of each thermal dissolution tank 1 is provided with a slag discharge port, insoluble impurities contained in waste plastics are discharged from the slag discharge port, the lower part of each thermal dissolution tank 1 is provided with a thermal solution outlet, and then the waste plastics and oil materials are thermally dissolved to form a thermal solution which can enter the next unit for operation and reaction.
Specifically, the device further comprises a catalytic reaction unit for performing catalytic reaction on the hot solution formed by the hot dissolution unit, and the hot dissolution unit is connected with the catalytic reaction unit, specifically, each hot dissolution tank 1 is communicated with the catalytic reaction unit through a feed pump 2.
Specifically, the catalytic reaction unit comprises a riser reactor, each hot dissolution tank is connected with the riser reactor 4 through a feed pump 2, so that hot dissolution liquid is fed into a lower inlet of the riser reactor of the catalytic reaction unit from a hot melt liquid outlet at the lower part of the hot dissolution tank through the feed pump 2, and goes up along the riser reactor and undergoes catalytic cracking or catalytic cracking reaction.
The catalytic reaction unit comprises a stripper 5 and a settler 6, wherein two ends of the stripper 5 are respectively connected with the riser reactor and the settler 6, products after the reaction of the riser enter the settler 6 to realize separation of high coke catalyst and other reaction products, and the high coke catalyst descends to the stripper 5 of the catalytic reaction unit in the settler 6 under the action of gravity and is stripped.
The device also comprises a waste activated carbon feeder 3, wherein the waste activated carbon feeder 3 is communicated with the settler 6, so that waste activated carbon and/or waste activated coke are sent into the settler 6 of the catalytic reaction unit through the activated carbon feeder in an inert gas atmosphere and are mixed with the catalyst, reactants and products from the reverse riser reactor. The highly coked catalyst (spent catalyst) and solid particles such as spent activated carbon and/or spent activated coke formed after completion of the reaction are gravity fed in a settler 6 to a stripper 5 of the catalytic reaction unit. Wherein the entrained and adsorbed oil gas comprising VOCs is stripped by steam from the bottom of the stripper 5 and leaves the settler 6 along with the reaction product to a product separation system for recovering petrochemical products such as olefins, aromatic hydrocarbons and oils.
The device also comprises a coke burning unit which is connected with the catalytic reaction unit. Specifically, the coke burning unit includes a coke burner 7, and a catalyst inlet of the coke burner 7 communicates with a catalyst outlet of the stripper through a spent chute 8. Then, the highly coked catalyst (spent catalyst) and the waste activated carbon and/or waste activated coke formed by the catalytic reaction unit flow into the coke burner 7 through the spent inclined tube 8 after other oil gas (containing VOCs) is removed by the stripper 5, and burn with air from the bottom of the coke burner 7 at high temperature (590-750 ℃) in a fluidization state, and the generated flue gas is discharged after being treated by the flue gas energy recovery and purification system.
The catalyst outlet of the coke burner 7 is communicated with the catalyst inlet of the riser reactor through a regeneration inclined tube 9, then the high coke catalyst (spent catalyst) is converted into the low coke catalyst (regenerated catalyst) after passing through the coke burner 7, and the low coke catalyst is recycled to the bottom of the riser reactor through the regeneration inclined tube 9 and the hot dissolved liquid of the waste plastics and oil products for continuous reaction.
In fig. 1, a represents oil; b represents waste plastics; c represents an inert gas; d represents waste activated carbon; e represents water vapor; f represents air.
In a second aspect, the present utility model provides a system for simultaneously treating waste plastics and waste active adsorbent material comprising the apparatus for simultaneously treating waste plastics and waste active adsorbent material described above.
The embodiment also provides the specific use process of the device for simultaneously treating the waste plastics and the waste active adsorption material:
waste plastics are sent into a thermal dissolution tank 1 in an inert gas atmosphere, and are thermally dissolved with oil materials with the temperature of 180-310 ℃ under the stirring state; HCl, HF and NH produced during dissolution 3 The corrosive gas is stripped from the inert gas entering from the lower part of the thermal dissolution tank 1 and sent to the corrosive gas treatment system.
Insoluble impurity components contained in the waste plastics are discharged from the thermal dissolution unit through a slag discharge port at the bottom of the thermal dissolution tank 1. The solution produced after the thermal dissolution of the waste plastics and the oil products is sent into the inlet of the lower part of the riser reactor 4 of the catalytic reaction unit from the outlet of the middle lower part of the thermal dissolution tank 1 through the feed pump 2, contacts with the high-temperature (590-750 ℃) low-coke catalyst (regenerated catalyst) from the coke burner 7, goes upward along the riser reactor 4 and undergoes catalytic cracking/decomposition reaction, and then enters the settler 6 at the upper part of the catalytic reaction unit to realize the separation of the catalyst and the reaction products.
The waste active carbon and/or waste active coke is sent into a settler 6 at the upper part of the catalytic reaction unit through a feeder in the inert gas atmosphere, and is mixed with the catalyst, reactants and products with the temperature between 470 and 580 ℃ from the outlet of the riser reactor 4.
The high coke catalyst (spent catalyst) and solid particles of spent activated carbon and/or spent activated coke formed after completion of the reaction are gravity-fed in a settler 6 to a stripper 5 of the catalytic reaction unit. Wherein the entrained and adsorbed oil gas comprising VOCs is stripped by steam from the bottom of the stripper 5 and leaves the settler 6 along with the reaction product to a product separation system for recovering petrochemical products such as olefins, aromatic hydrocarbons and oils.
After stripping and removing oil gas (containing VOCs) from high coke catalyst (spent catalyst) and waste active carbon and/or waste active coke, the high coke catalyst (spent catalyst) and waste active coke flow into a coke burner 7 (catalyst regenerator) through a spent inclined tube 8, and are combusted with air from the bottom of the coke burner 7 at high temperature (590-750 ℃) in a fluidization state, and the generated flue gas is discharged after being treated by a flue gas energy recovery and purification system.
The waste active carbon and/or waste active coke is burnt with air in a coke burner 7 to generate flue gas and trace dust, and the flue gas and trace dust are discharged along with the burning flue gas; the high coke catalyst (spent catalyst) is converted into low coke catalyst (regenerated catalyst) through a coke burner 7, and then is recycled to the bottom of the riser reactor through a regeneration inclined tube 9 to react with the dissolved liquid of the waste plastics and oil products continuously.
Examples 2 to 3 and comparative examples 1 to 3
Examples 2-3 and comparative examples 1-3 provide examples of specific applications of the device of example 1, using the specific specifications of the device of example 1 as follows: wherein the mixed liquor throughput (flow rate of the feed pump 2) of the apparatus was 5kg/h. The inner diameter of the riser reactor 4 of the catalytic reaction unit is 16mm, the height is 3200mm, the inner diameter of the settler 6 of the catalyst is 160mm, the height is 800mm, and the inner diameter of the stripper 5 of the catalyst is 120mm, the height is 700mm. The inner diameter of the upper dilute phase section of the coke burner 7 of the coke burning unit of the device is 260mm, the height is 600mm, the lower dense phase Duan Najing is 100mm, and the height is 650mm. The solid activated carbon feeding amount of the activated feeder 3 of the device is 100-300g/h. The inner diameters of the waiting inclined tube 8 and the regenerating inclined tube 9 are 12mm. The device has small scale and large heat dissipation capacity, and the temperature rise and the heat preservation of the device are all heated by electricity in order to realize the heat balance of the device.
The waste plastics used in examples and comparative examples were GDG-05 waste plastic particles purchased through the market, and their physicochemical properties are shown in Table 1; the waste activated carbon used in examples and comparative examples was waste activated carbon samples CC-01 and MC-02 collected by R coating company and Z machine factory, and the physicochemical properties thereof are shown in Table 2. The oils used in the examples and comparative examples were heavy oils and catalytic slurries obtained from Ningxia silver mountain energy chemical industry Co., ltd, and their physicochemical properties are shown in Table 3. The catalysts used in the examples and comparative examples were heavy oil catalytic cracking equilibrium catalysts obtained from Ningxia silver mountain energy chemical industry Co., ltd, and their physicochemical properties are shown in Table 4.
TABLE 1 composition and Properties of waste plastics
* Ash is mainly the filler component calcium carbonate in plastic articles.
TABLE 2 composition and Properties of waste activated carbon
* The VOCs consisted of toluene 75% wt and n-butanol 25% wt.
TABLE 3 physicochemical Properties of heavy oil
TABLE 4 catalytic cracking catalyst Properties
| Project | CGP-1 equilibrium catalyst |
| Micro-inverse Activity,% | 61 |
| Specific surface, m 2 /g | 108 |
| Pore volume, ml/g | 0.13 |
| Bulk density, kg/m 3 | 0.87 |
| Average particle diameter, μm | 60.25 |
| Carbon content, wt% | 0.05 |
| Chemical composition, wt% | |
| SiO 2 | 48.96 |
| Al 2 O 3 | 40.22 |
| La 2 O 3 | 1.33 |
| Metal content, μg/g | |
| Na | 700 |
| Fe | 3230 |
| Ni | 4898 |
| V | 2560 |
Dechlorination:
thermal dissolution and dechlorination of waste plastics and heavy oil. 160 kg of heavy oil is added into a 300 liter enamel dissolution tank which is provided with a steam inlet at the bottom, a hot water condensation reflux outlet at the top and a stirrer at the inside and is heated by 300 liter of heat conducting oil, and the mixture is heated while stirring at a stirring speed of 300rpm and a heating speed of 5 ℃/min, and when the temperature rises to 190 ℃, 40 kg of waste plastic GDC-05 is added into the dissolution tank at a speed of 10 kg/min. And simultaneously continuing stirring and heating, sampling and analyzing the completely dissolved liquid when the temperature rises to 220 ℃, and then opening a water vapor inlet valve at the bottom of the dissolution tank and a circulating condensate water valve of a reflux device at the top of the dissolution tank, wherein saturated water vapor of 0.35MPa enters the dissolution liquid from the bottom of the dissolution tank at a rate of 5 liters/min. And (3) continuously stirring and heating the dissolved liquid in the dissolution tank, carrying out steam stripping until the temperature reaches 320 ℃, stopping heating, continuously introducing steam and carrying out steam stripping for 10 minutes, and obtaining the purified mixed dissolved liquid in the dissolution tank. An aqueous solution of hydrogen chloride (dilute hydrochloric acid) was obtained at the top outlet of the dissolution tank. After dissolution and dechlorination, the dechlorinated dissolution liquid is sampled and analyzed. The analysis results are shown in Table 5.
TABLE 5 elemental composition of waste Plastic and heavy oil solutions before and after dechlorination
| Sample name | C*，wt％ | H，wt％ | S，wt％ | N，wt％ | Cl，wt％ |
| Solution before dechlorination | 84.29 | 12.06 | 0.54 | 0.24 | 0.23 |
| Solution after dechlorination | 84.66 | 12.11 | 0.54 | 0.26 | 0.001 |
* Excluding carbon in calcium carbonate.
From the experimental results and the analysis data in Table 5, it can be seen that the waste plastics GDC-05 and the heavy oil in Table 3 can be completely mutually dissolved into a uniform fluid liquid material at 190-220 ℃ for 20 minutes, the liquid material can be completely decomposed into HCl in the slow temperature rising process of 220-320 ℃, the chlorine element removal rate of the mixed liquid is 99.57%, and the corrosion of the element chlorine to processing equipment in the subsequent processing is greatly relieved.
Specifically, CGP-1 equilibrium catalyst shown in Table 4, dechlorinated dissolution solution, and waste activated carbon CC-01 shown in Table 2 were used. The amount of the waste activated carbon added was 50g/h, and the other process operation conditions of the medium-sized experimental device are shown in Table 6. The experimental results data are presented in table 7.
Table 6 main operating conditions of the experimental set-up
Table 7 comparison of experimental results
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Comparison of the experimental conditions of Table 6 with the experimental results of Table 7 can be seen:
the mixed liquid of 1.20% waste plastic GDC-05 and 80% heavy oil (example 2 and example 3) has the advantages that the yield of the low-carbon olefin (ethylene+propylene+butylene) obtained by catalytic cracking can be increased from 15.16wt% to 20.42wt% and 34.70% compared with the pure heavy oil (comparative examples 1-3). In addition to the low olefins, the waste plastics crack to produce a portion of light paraffins and aromatics rich (BTEX) gasoline. The process method provided by the utility model can effectively convert waste plastics into petrochemical raw materials such as low-carbon olefin, light aromatic hydrocarbon, oil products and the like, hydrogen and methane are not generated by cracking the waste plastics in the process, the coking rate is far lower than that of heavy oil raw materials, and the process method is an ideal effective way for treating the waste plastics.
2. Compared with the single processing of pure heavy oil (comparative example 3), the mixed liquid of waste active carbon, 20% waste plastic GDC-05 and 80% heavy oil is treated by adopting the process method (examples 2-3 and comparative examples 1-2), on one hand, the VOCs resources contained in the waste active carbon can be fully and effectively recovered, and on the other hand, the heat released by the combustion of the VOCs waste active carbon entering the coke burning unit is removed in the reaction unit, and the heat required by the catalytic reaction unit for cracking the waste plastic and/or heavy oil can be used. The effect is quite obvious from the power consumption indexes of the above examples 2-3 and comparative examples 1-3, and the added waste activated carbon is increased from 0 g/hr (comparative example 3) to 50 g/hr (comparative example 1) to 200 g/hr (comparative example 2), and the power consumption E4 of the coke burner 7 is decreased from 1854W to 1417W to 106W. While the heat of combustion of the waste activated carbon was utilized by the waste plastic cracking reaction, this result was directly reflected in the data (e1+e2+e3-E4) of the two sets of comparison (power consumption of coke burner 7-power consumption of catalytic reaction unit riser reactor, catalyst settler 6 and catalyst stripper 5) of example 2 and comparative example 1, example 3 and comparative example 2.
3. The heat generated by burning the coke generated by cracking the waste activated carbon and the waste plastic is taken away by the flue gas, and sulfur, nitrogen and solid impurities in the waste plastic and the waste activated carbon can be further recovered and purified by a flue gas energy recovery and purification system, so that the technical route of the utility model is realized, and the environment-friendly technical essence is maintained while resources are recovered.
The above description is only of the preferred embodiments of the present utility model and is not intended to limit the present utility model, and various modifications and variations may be made to the present utility model by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present utility model should be included in the protection scope of the present utility model.
Claims (10)
1. The device for simultaneously treating the waste plastics and the waste active adsorption materials is characterized by comprising a thermal dissolution unit for thermally dissolving the waste plastics and the oil, a catalytic reaction unit for carrying out catalytic reaction on a thermal solution formed by the thermal dissolution unit and a coke burning unit for burning, wherein the thermal dissolution unit, the catalytic reaction unit and the coke burning unit are sequentially connected.
2. The apparatus for simultaneously treating waste plastic and waste active adsorbing material according to claim 1, wherein said thermal dissolving unit comprises a thermal dissolving tank which is in communication with said catalytic reaction unit via a feed pump.
3. The apparatus for simultaneously treating waste plastics and waste active adsorbing materials according to claim 2, wherein the number of said thermal dissolving tanks is plural, a plurality of said thermal dissolving tanks are arranged in parallel, and each of said thermal dissolving tanks is communicated with said catalytic reaction unit by said feed pump.
4. A device for simultaneously treating waste plastics and waste active adsorption materials according to claim 2 or 3, wherein a stirring part is arranged in each thermal dissolution tank, an inert gas inlet is arranged at the bottom of each thermal dissolution tank, a corrosive gas outlet is arranged at the top of each thermal dissolution tank, a slag discharge port is arranged at the bottom of each thermal dissolution tank, oil and waste plastics inlets are arranged at the upper part of each thermal dissolution tank, and a hot solution outlet is arranged at the lower part of each thermal dissolution tank.
5. The apparatus for simultaneously treating waste plastics and waste active adsorbent materials according to claim 1, wherein said catalytic reaction unit comprises a settler, a stripper and a riser reactor connected in sequence, said thermal dissolution unit being in communication with a hot solution inlet of said riser reactor via a feed pump, said riser reactor and said stripper both being in communication with said coke burning unit.
6. The apparatus for simultaneously processing waste plastic and waste activated adsorbent material of claim 5, further comprising a waste activated carbon feeder in communication with said settler.
7. The apparatus for simultaneous treatment of waste plastics and waste active adsorbent material according to claim 5, wherein said coke burning unit comprises a coke burner, a catalyst outlet of said coke burner being in communication with a catalyst inlet of said riser reactor via a regeneration chute.
8. The apparatus for simultaneous treatment of waste plastics and waste active adsorbent material according to claim 7, wherein the catalyst inlet of said coke burner is in communication with the catalyst outlet of said stripper via a spent chute.
9. The apparatus for simultaneously treating waste plastic and waste active adsorbing material according to claim 7, wherein the bottom of said coke burner is provided with a gas inlet.
10. A system for simultaneous treatment of waste plastics and waste active adsorbent material, characterised in that it comprises a device for simultaneous treatment of waste plastics and waste active adsorbent material according to any one of claims 1-9.
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