CN111218307A - Method for converting material containing polycarbonate compound into cyclic hydrocarbon in aviation kerosene - Google Patents
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Abstract
The invention relates to a method for synthesizing cyclic hydrocarbon in aviation kerosene by using material containing polycarbonate compound. The disadvantage of low density in the biomass aviation fuel obtained by the prior art is solved. Because the plastic, plate and glass made of waste polycarbonate are low in cost, and the plastic and glass made of waste polycarbonate have great threat to the environment as white garbage. Therefore, the method not only solves the aviation fuel problem to a certain extent, but also solves the environmental problem caused by white pollution. Has potential advantages in future industrial applications.
Description
Technical Field
The invention relates to a method for directly converting waste plastic, plate and glass made of polycarbonate into aviation kerosene range cyclic hydrocarbon. The method specifically comprises the following two steps: 1) carbon is collected from the wasteMixing plastic, plate and glass made of acid ester with alcohol, and carrying out alcoholysis at high temperature to obtain aromatic diol; 2) hydrodeoxygenation of the aromatic diol generated in the step 1 to obtain C13-15Of (a) an alkane. The method is a method for directly converting plastic, plates and glass manufactured by waste polycarbonate into aviation fuel for the first time at present, compared with the traditional aviation fuel, the raw material sources are cheap and easy to obtain, and the plastic and glass manufactured by the waste polycarbonate in life can be directly used without pretreatment.
Background
The environmental problems such as the decrease of fossil resources and the emission of greenhouse gases caused by the combustion of fossil energy are highlighted, the social demand of energy is continuously increased, the price of petroleum is continuously increased, and the development of new energy capable of replacing fossil resources and the development of new channels for supplying renewable fuel oil are imperative.
The international demand of aviation kerosene is increasing as a strategic material in a country. The aviation kerosene is generally composed of alkanes with 6-16 carbon atoms. The great development of renewable aviation kerosene technology has profound strategic significance from the aspects of national energy safety and potential economic value. The biological aviation kerosene synthesized by the international prior art mainly takes chain hydrocarbon as the main chemical structure, is lower than the traditional aviation kerosene (mixture of chain hydrocarbon, cycloparaffin and aromatic hydrocarbon) in the aspects of density (volume heat value) and sealing property, and can meet the performance requirement of aviation fuel only by being mixed with the traditional aviation kerosene.
With the rapid development of national economy, the plastic industry has gained rapid development, and plastic materials are favored by various fields by virtue of excellent properties thereof. At present, waste plastics increase year by year, and how to treat the waste plastics based on energy utilization and environmental protection becomes a focus of social attention. The reasonable disposal and safe disposal of the waste plastics belong to the environmental protection problem worldwide, and are important for the basic national policy of environmental protection, the improvement of the quality of living environment and the technical research of the environment-friendly disposal process of the waste plastics. China is a big country for producing waste plastics, and the treatment of recycling garbage is urgent. The waste plastics in China mainly come from plastic bags, agricultural and domestic plastic films, foams, domestic and industrial plastic products and the like. According to incomplete statistics, the yield of plastics in China per year is up to ten million tons, the annual waste plastic amount accounts for about 6 days, and the annual waste plastic amount is increased year by year. In addition, most of the waste plastics are engineering waste plastics, and due to the fact that the waste plastics are various in types and large in quantity, huge pressure is caused to the society and the environment.
At present, the following methods are mainly used for recycling and utilizing waste plastics: 1) simple recovery treatment of waste plastics refers to the classified recovery of production and living waste plastics, and then direct utilization or processing, production and recycling are carried out. Simple recycling of waste plastics is the most aggressive means of material recycling and is the most effective method of environmentally friendly disposal. 2) The composite regeneration processing is used for recycling waste plastics in the market and recycling plastics produced in the production and living circulation of the market such as commerce, industry, agriculture, civilian use and the like. Mainly comprises the working procedures of shearing, rolling, remolding and the like. The composite regeneration of the waste plastics not only effectively reduces the production cost of production enterprises, but also plays a more prominent role in environmental protection. 3) The sanitary landfill treatment is a treatment mode with the minimum added value, the recycling value of the waste plastic is wasted, the land resources are occupied in a large area, and in addition, the sanitary landfill treatment still needs certain safety technology. 4) The incineration method is used for recovering heat, waste plastics are fuel with higher heat value, and the waste plastics are treated in a treatment mode with higher added value by the incineration method, but the problem of secondary pollution needs to be solved. Therefore, the plastic needs to be screened according to different components, and an incineration exhaust gas treatment device needs to be additionally arranged. 5) The photodecomposition technology is that a photodecomposition promoting substance, such as a photosensitizer and the like, is added in the production process of plastics, and the plastics are subjected to photodecomposition treatment by light. The main treatment object of the photodecomposition technology is a metal-containing plastic product, so that the pollution of heavy metals to water, air or soil is reduced. 6) The biochemical method comprises adding starch and related substances into pretreated waste plastics, and treating with microorganismThe main points are to reduce the strength of the plastic and reduce the content of harmful substances. But the requirement of biological decomposition treatment is high, the cost is high, and the biological decomposition treatment is not popularized and used. 7) The chemical treatment method is to generally convert waste plastics into small molecules through pyrolysis, alcoholysis and hydrolysis, and then further convert and utilize the small molecules to obtain products with higher economic added value. PC resin is one of five common engineering plastics in the world at present. The PC plastic has high film forming property and formation property, good optical transparency, excellent abrasion and friction resistance, dimensional stability and electrical insulation property. Three major application fields of PC engineering plastics are the glass assembly industry, the electronics industry, the electrical appliance industry, and further industrial mechanical parts, optical disks, packaging, computers and other office equipment, medical treatment and health care, films, leisure and protection equipment and the like. PC can be used as door and window glass, and PC laminated plates are widely used for protective windows of banks, embassys and public places, and are used for airplane cabin covers, lighting equipment, industrial safety barriers and bulletproof glass, so far, no relevant report of synthesizing aviation kerosene range cyclic hydrocarbon by using waste PC resin is provided internationally. The invention selectively synthesizes C by utilizing the waste PC resin through catalytic conversion13-C15The aviation kerosene range cyclic hydrocarbon not only can change waste into valuable, reduce environmental pollution, solve the problems existing in the aspect of volume heat value of the prior biological aviation kerosene and the prior aviation kerosene, and has very important practical value.
Disclosure of Invention
The invention aims to provide a method for directly converting waste polycarbonate-made plastics, plates and glass into aviation kerosene-range cyclic hydrocarbon
The invention is realized by the following technical scheme:
mixing a material containing a polycarbonate compound with alcohol, carrying out alcoholysis at high temperature to obtain aromatic diol, and finally converting the aromatic diol into C under the catalysis of a hydrodeoxygenation catalyst13-C15The desired alkane in the aviation kerosene of (a);
the polycarbonate compound is one or two of polycarbonate bisphenol A ester (bisphenol A polycarbonate) and polycarbonate bisphenol F ester (bisphenol F polycarbonate).
The alcohol is: one or more of methanol, ethanol, propanol, butanol, ethylene glycol, propylene glycol and glycerol, wherein the mass ratio of the polycarbonate compound to the alcohol is 10 to 0.001, preferably 1 to 0.001, and more preferably 0.5 to 0.001.
The hydrodeoxygenation catalyst is one or more than two of the following supported catalysts or non-supported catalysts:
unsupported catalysts: one or more than two of active carbon, silicon oxide, aluminum oxide, titanium oxide, zirconium oxide, molecular sieve, Raney nickel, Raney cobalt, Raney iron and Raney copper;
the supported catalyst: the supported catalyst is prepared by taking one or more than two of active carbon, silicon oxide, aluminum oxide, titanium oxide, zirconium oxide and molecular sieve as a carrier, and the active component carried in the supported catalyst is one or more than two of metals of Pt, Ru, Pd, Rh and Ir.
The hydrodeoxygenation supported catalyst is prepared by adopting an isometric impregnation mode: uniformly mixing a soluble metal compound solution with the mass concentration of 0.01-50% with a carrier, standing for 4-12 h at normal temperature, drying for 4-12 h at the temperature of 60-120 ℃, roasting for 1-6 h at the temperature of 200-600 ℃, reducing for 1-6 h at the temperature of 100-400 ℃ in a hydrogen atmosphere, and finally adding 0.1-10% of O in terms of volume ratio2/N2Passivating for 0.5-12 h in the mixed atmosphere.
The hydrodeoxygenation supported catalyst comprises: the mass ratio of the active metal to the carrier is 0.001 to 0.5, preferably 0.01 to 0.2, and more preferably 0.02 to 0.1.
For the hydrodeoxygenation process, it is carried out in a solvent: the solvent is one or more of hexane, cyclohexane, heptane, octane, nonane and decane.
For the alcoholysis process: the alcoholysis reaction is carried out in a reaction kettle, the reaction temperature is 100-300 ℃, the preferable temperature is 120-300 ℃, the more preferable temperature is 150-300 ℃, the reaction time is 0.5-10 hours, the preferable time is 1-10 hours, and the more preferable time is 2-10 hours.
For the hydrodeoxygenation process: the hydrogenation reaction is carried out in a reaction kettle, the reaction temperature is 50-260 ℃, the preferred temperature is 100-260 ℃, the more preferred temperature is 120-260 ℃, the mass ratio of the catalyst to the aromatic diol is 0.01-0.5, the preferred mass ratio is 0.02-0.4, the more preferred mass ratio is 0.03-0.3, the mass ratio of the aromatic diol to the solvent is 0.01-0.5, the preferred mass ratio is 0.02-0.4, the more preferred mass ratio is 0.03-0.3, the reaction time is 0.5-24 hours, the preferred reaction time is 1-24 hours, the more preferred reaction time is 2-24 hours, the hydrogen pressure is 0.1-8 MPa, the preferred pressure is 0.5-8 MPa, and the more preferred pressure is 1-8 MPa.
The material containing the polycarbonate compound is one or more than two of plastic and glass manufactured by adopting the polycarbonate compound.
The invention has the following advantages:
the method for directly converting the polycarbonate manufacturing substances into the aviation kerosene range cyclic hydrocarbon has the characteristics of cheap and easily-obtained raw materials, simple synthesis method and high substrate universality, and can obtain polycyclic hydrocarbon components which are lacked by the traditional biomass aviation kerosene, and the density of the aviation kerosene can be improved by the aromatic hydrocarbon polycyclic hydrocarbon. On the other hand, the method can reduce white pollution from the aspect of environment, and not only solves the energy problem to a certain extent, but also solves the environmental problem to a certain extent. Therefore, the method has a promising development prospect.
Drawings
FIG. 1 is a chemical structural diagram of a waste polycarbonate-based plastic.
FIGS. 2-5 are chemical structural diagrams of a series of intermediates, detailed as follows:
FIG. 2 is a chemical structural diagram of bisphenol A;
FIG. 3 is a chemical structural diagram of bisphenol F;
FIG. 4 is a chemical structural diagram of dimethyl carbonate;
FIG. 5 is a chemical structural diagram of diethyl carbonate;
FIG. 6 is a chemical structural diagram of propylene carbonate;
FIG. 7 shows a chemical structure of ethylene carbonate.
FIGS. 8-10 are chemical structural diagrams of the final aviation fuel components, detailed below:
FIG. 8.C13Chemical structure of bicycloalkane;
FIG. 9.C13Chemical structure diagram of tricycloalkane;
FIG. 10.C15Chemical structure of bicycloalkane.
Detailed Description
The invention will now be illustrated by means of specific examples, without restricting its scope to these examples.
Examples
1. And (3) investigating the reaction activity under each reaction condition in the polycarbonate alcoholysis process.
1.1 influence of the reaction temperature during the alcoholysis of polycarbonates. Reaction conditions are as follows: 1g of bisphenol A polycarbonate, 40g of methanol, reaction time: 3.5 h. See Table 1
TABLE 1 different reaction temperatures
As seen from Table 1, as the reaction temperature increased, the conversion of polycarbonate bisphenol A ester gradually increased, and the yield of bisphenol A also gradually increased until the highest conversion was reached at 180 ℃.
1.2 influence of the reaction time in the alcoholysis process of polycarbonates. Reaction conditions are as follows: 1g of bisphenol A polycarbonate, 40g of methanol, reaction temperature: 180 ℃ is carried out. See Table 2
TABLE 2 different reaction times
As can be seen from Table 2, the yield of bisphenol A gradually increased with the increase of the reaction time, but did not increase any more when the reaction time exceeded 5 hours.
1.3 influence of the polycarbonate to methanol mass ratio during the alcoholysis of polycarbonates. Reaction conditions are as follows: 0.1g of bisphenol F polycarbonate, reaction time: 3.5h, reaction temperature: 180 ℃ is carried out. See Table 3
TABLE 3 influence of the mass ratio of different polycarbonates to methanol
As seen from Table 3, when the mass ratio of bisphenol F polycarbonate to methanol was increased to 50%, the yield of bisphenol F gradually decreased.
1.3 influence of different alcohols in the alcoholysis of polycarbonates. Reaction conditions are as follows: 1g of bisphenol F polycarbonate, mass of alcohol: 40g, reaction time: 3.5h, reaction temperature: 180 ℃ is carried out. See Table 4
TABLE 4 influence of different alcohols
As can be seen from Table 4, the alcoholysis of the polycarbonate was carried out with different alcohols, methanol and ethanol being the most effective. 2. And (3) investigating the reactivity of the monomers (bisphenol A and bisphenol F) subjected to polyester alcoholysis under various reaction conditions in the hydrodeoxygenation process. 2.1 the activity of the metal supported catalyst obtained by different preparation methods in the process of hydrodeoxygenation of monomer bisphenol A after polyester alcoholysis is not considered. Reaction conditions are as follows: 1g of bisphenol A,40g of octane, 0.04g of a metal catalyst, 0.04g H-ZSM-5 type molecular sieve, hydrogen pressure: 5MPa, reaction temperature: 160 ℃, reaction time: 3.5 h. See tables 5-13
TABLE 5 catalysts supported on different metals
Note: minus prepared in Table 5The supported catalyst was prepared using the following conditions: mixing 5% metal ion solution with 1g carrier, standing at room temperature for 8 hr to control the mass ratio of metal ion to carrier at 5%, drying at 120 deg.C for 10 hr, calcining at 500 deg.C for 4 hr, reducing at 300 deg.C in hydrogen atmosphere for 2 hr, and adding 1% O2/N2Passivating for 4 hours under the mixed atmosphere of (1).
As can be seen from table 5, different metal supported activated carbon catalysts have a great difference in catalytic activity for this hydrogenation process, with platinum metal having the highest conversion and yield.
TABLE 6 influence of different Metal loadings on catalyst Activity
Note: the catalysts prepared in table 6 were prepared using the following conditions: mixing 5% solution containing platinum ion with 1g carrier, standing at room temperature for 8 hr, drying at 120 deg.C for 10 hr, calcining at 500 deg.C for 4 hr, reducing at 300 deg.C under hydrogen atmosphere for 2 hr, and adding 1 vol% O2/N2Passivating for 4 hours under the mixed atmosphere of (1).
As can be seen from Table 6, the activity of the catalyst gradually increased with the increase in the metal loading, but did not increase any more when the loading was increased to 5%, indicating that the active sites on the catalyst also gradually increased with the increase in the metal loading within a certain range.
TABLE 7 influence of different standing times on the catalytic activity synthesized
Note: the catalysts prepared in table 7 were prepared using the following conditions: mixing the solution containing 5% platinum ion with 1g of carrier uniformlyStanding at room temperature to control the mass ratio of metal ions to carrier at 5%, drying at 120 deg.C for 10 hr, calcining at 500 deg.C for 4 hr, reducing at 300 deg.C in hydrogen atmosphere for 2 hr, and adding 1 vol% O2/N2Passivating for 4 hours under the mixed atmosphere of (1).
As seen from Table 7, different standing times have some influence on the catalytic activity of the prepared catalyst, but the standing time exceeding 4 hours hardly has an influence.
TABLE 8 influence of catalyst drying temperature on the activity of the synthesized catalyst
Note: the catalysts prepared in table 8 were prepared using the following conditions: mixing a solution containing 5% platinum ions with 1g of carrier, standing at room temperature for 8h to control the mass ratio of metal ions to carrier at 5%, drying for 10h, calcining at 500 deg.C for 4h, reducing at 300 deg.C in hydrogen atmosphere for 2h, and adding 1% by volume of O2/N2Passivating for 4 hours under the mixed atmosphere of (1).
As can be seen from Table 8, different drying temperatures have some effect on the hydrogenation activity of the catalyst, but have little effect when the temperature exceeds 70 ℃.
TABLE 9 influence of catalyst drying time on the activity of the synthesized catalyst
Note: the catalysts prepared in table 9 were prepared using the following conditions: mixing solution containing platinum ion 5% with 1g carrier, standing at room temperature for 8 hr to control the mass ratio of metal ion to carrier at 5%, drying at 120 deg.C, calcining at 500 deg.C for 4 hr, reducing at 300 deg.C for 2 hr in hydrogen atmosphere, and adding 1 vol% of O2/N2Passivating for 4 hours under the mixed atmosphere of (1).
As can be seen from Table 9, the drying time had substantially no effect on the activity of the prepared catalyst when the drying time exceeded 3 hours.
TABLE 10 Effect of calcination temperature on the Activity of the synthesized catalyst
Note: the catalysts prepared in table 10 were prepared using the following conditions: mixing a solution containing 5% platinum ion with 1g of carrier, standing at room temperature for 8h to control the mass ratio of metal ion to carrier at 5%, drying at 120 deg.C for 10h, calcining at high temperature for 4h, reducing at 300 deg.C for 2h in hydrogen atmosphere, and adding 1% by volume of O2/N2Passivating for 4 hours under the mixed atmosphere of (1).
As can be seen from Table 10, the calcination temperature has a significant effect on the catalyst activity, and as the temperature is increased, the catalyst activity is significantly increased until it is substantially unchanged after exceeding 500 ℃.
TABLE 11 Effect of calcination time on the activity of the synthesized catalyst
Note: the catalysts prepared in table 11 were prepared using the following conditions: mixing a solution containing 5% platinum ion with 1g of carrier, standing at room temperature for 8h to control the mass ratio of metal ion to carrier at 5%, drying at 120 deg.C for 10h, calcining at 500 deg.C, reducing at 300 deg.C in hydrogen atmosphere for 2h, and adding 1% by volume of O2/N2Passivating for 4 hours under the mixed atmosphere of (1).
As can be seen from Table 11, the catalyst activity gradually increased with the increase in the calcination time in 1 to 4 hours, and the catalyst activity remained substantially unchanged even with the increase in the calcination time in 4 to 7 hours. And when the calcination time was extended to 7 hours, the catalyst activity gradually decreased with the extension of the calcination time.
TABLE 12 influence of catalyst reduction temperature on the activity of the synthesized catalyst
Note: the catalysts prepared in table 12 were prepared using the following conditions: mixing a solution containing 5% platinum ion with 1g of carrier, standing at room temperature for 8h to control the mass ratio of metal ion to carrier at 5%, drying at 120 deg.C for 10h, calcining at 500 deg.C for 4h, reducing in hydrogen atmosphere for 2h, and adding 1% by volume of O2/N2Passivating for 4 hours under the mixed atmosphere of (1).
As can be seen from table 12, the catalyst activity gradually increased with the increase in the catalyst reduction temperature, and the catalyst reduction temperature had substantially no effect on the activity thereof when the temperature was increased to 250 ℃.
TABLE 13 influence of catalyst reduction time on the activity of the catalysts synthesized
Note: the catalysts prepared in table 13 were prepared using the following conditions: mixing a solution containing 5% platinum ion with 1g of carrier, standing at room temperature for 8h to control the mass ratio of metal ion to carrier at 5%, drying at 120 deg.C for 10 hr, calcining at 500 deg.C for 4 hr, reducing at 300 deg.C in hydrogen atmosphere, and adding 1% by volume of O2/N2Passivating for 4 hours under the mixed atmosphere of (1).
As can be seen from table 13, the catalyst activity increased with increasing reduction time from the catalyst.
2.2 investigating the influence of reaction conditions in the process of hydrodeoxygenation by monomer bisphenol F after polyester alcoholysis. Wherein the metal supported catalyst is prepared by adopting the following conditions: mixing a solution containing 5% platinum ion with 1g of carrier, standing at room temperature for 8h to control the mass ratio of metal ion to carrier at 5%, drying at 120 deg.C for 10h, calcining at 500 deg.C for 4h, reducing at 300 deg.C for 2h in hydrogen atmosphere, and adding 1% by volume of O2/N2The passivation time is 4h under the mixed atmosphere, and the table is 14-18.
TABLE 14 influence of Supported catalyst quality on the hydrogenation Process
Note: reaction conditions in table 14: 1g of bisphenol F, 40g of cyclohexane, 5% Pt/C as catalyst, 180 ℃, 4h, hydrogen pressure: 5 MPa.
As can be seen from Table 14, the conversion of bisphenol F gradually increased with increasing mass of catalyst, and did not increase until 3g was reached.
TABLE 15 influence of different temperatures on the hydrogenation process
Note: reaction conditions in table 15: 1g bisphenol F, 40g hexane, 0.04g 5% Pt/C, 0.04g zirconia, 4h, hydrogen pressure: 5 MPa.
As can be seen from Table 15, the long bisphenol F was hydrogenated completely with the increase in temperature until the temperature was increased to 120 degrees, and the bisphenol F was completely hydrogenated.
TABLE 16 influence of reaction time on the hydrogenation process
Note: reaction conditions in table 16: 1g bisphenol F, 40g heptane, 0.04g 5% Pt/C, 0.04g silica, 180 ℃, hydrogen pressure: 5 MPa.
As can be seen from Table 16, the conversion of bisphenol F gradually increased with increasing reaction time, and remained constant until 8 hours later.
TABLE 17 influence of hydrogen pressure on the hydrogenation process
Note: reaction conditions in table 17: 1g of bisphenol F, 40g of nonane, 0.04g of 5% Pt/C, 0.04g of alumina, 180 ℃ and 4 hours.
As can be seen from Table 17, the hydrogen pressure has a significant effect on the hydrogenation process, with very low conversion of bisphenol F at pressures below 1MPa and rapidly increasing conversion when the pressure exceeds 2 MPa.
TABLE 18 influence of different solvent quality on the hydrodeoxygenation Process
Note: reaction conditions in table 18: 0.5g bisphenol F, a solvent of decane, 0.04g 5% Pt/C, 0.04g titanium oxide, 180 ℃ and 4 h.
As can be seen from Table 18, the quality of the solvent had a great influence on the hydrodeoxygenation process, and as the quality of the solvent increased, the conversion of bisphenol F gradually decreased.
Claims (9)
1. The method for synthesizing the cyclic hydrocarbon in the aviation kerosene by using the material containing the polycarbonate compound is characterized by comprising the following steps:
mixing a material containing a polycarbonate compound with alcohol, carrying out alcoholysis at high temperature to obtain aromatic diol, and finally converting the aromatic diol into C under the catalysis of a hydrodeoxygenation catalyst13-C15The desired alkane in the aviation kerosene of (a);
the polycarbonate compound is one or two of polycarbonate bisphenol A ester and polycarbonate bisphenol F ester.
2. The method of claim 1, wherein:
the alcohol is: one or more of methanol, ethanol, propanol, butanol, ethylene glycol, propylene glycol and glycerol, wherein the mass ratio of the polycarbonate compound to the alcohol is 10 to 0.001, preferably 1 to 0.001, and more preferably 0.5 to 0.001.
3. The method of claim 1, wherein:
the hydrodeoxygenation catalyst is one or more than two of the following supported catalysts or non-supported catalysts:
unsupported catalysts: one or more than two of active carbon, silicon oxide, aluminum oxide, titanium oxide, zirconium oxide, molecular sieve, Raney nickel, Raney cobalt, Raney iron and Raney copper;
the supported catalyst: the supported catalyst is prepared by taking one or more than two of active carbon, silicon oxide, aluminum oxide, titanium oxide, zirconium oxide and molecular sieve as a carrier, and the active component carried in the supported catalyst is one or more than two of metals of Pt, Ru, Pd, Rh and Ir.
4. The method of claim 3, wherein:
the hydrodeoxygenation supported catalyst is prepared by adopting an isometric impregnation mode: uniformly mixing a soluble metal compound solution with the mass concentration of 0.01-50% with a carrier, standing for 4-12 h at normal temperature, drying for 4-12 h at the temperature of 60-120 ℃, roasting for 1-6 h at the temperature of 200-600 ℃, reducing for 1-6 h at the temperature of 100-400 ℃ in a hydrogen atmosphere, and finally adding 0.1-10% of O in terms of volume ratio2/N2Passivating for 0.5-12 h in the mixed atmosphere.
5. The method according to claim 3 or 4, characterized in that:
the hydrodeoxygenation supported catalyst comprises: the mass ratio of the active metal to the carrier is 0.001 to 0.5, preferably 0.01 to 0.2, and more preferably 0.02 to 0.1.
6. The method of claim 1, wherein:
for the hydrodeoxygenation process, it is carried out in a solvent: the solvent is one or more of hexane, cyclohexane, heptane, octane, nonane and decane.
7. The method of claim 1, wherein:
for the alcoholysis process: the alcoholysis reaction is carried out in a reaction kettle, the reaction temperature is 100-300 ℃, the preferable temperature is 120-300 ℃, the more preferable temperature is 150-300 ℃, the reaction time is 0.5-10 hours, the preferable time is 1-10 hours, and the more preferable time is 2-10 hours.
8. The method according to claim 1 or 6, characterized in that:
for the hydrodeoxygenation process: the hydrogenation reaction is carried out in a reaction kettle, the reaction temperature is 50-260 ℃, the preferred temperature is 100-260 ℃, the more preferred temperature is 120-260 ℃, the mass ratio of the catalyst to the aromatic diol is 0.01-0.5, the preferred mass ratio is 0.02-0.4, the more preferred mass ratio is 0.03-0.3, the mass ratio of the aromatic diol to the solvent is 0.01-0.5, the preferred mass ratio is 0.02-0.4, the more preferred mass ratio is 0.03-0.3, the reaction time is 0.5-24 hours, the preferred reaction time is 1-24 hours, the more preferred reaction time is 2-24 hours, the hydrogen pressure is 0.1-8 MPa, the preferred pressure is 0.5-8 MPa, and the more preferred pressure is 1-8 MPa.
9. The method of claim 1, wherein: the material containing the polycarbonate compound is one or more than two of plastic and glass manufactured by adopting the polycarbonate compound.
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| CN115073253A (en) * | 2021-03-15 | 2022-09-20 | 中国科学院大连化学物理研究所 | Method for synthesizing dicycloalkane by polycarbonate plastic in one step |
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| CN114181726A (en) * | 2020-09-15 | 2022-03-15 | 中国科学院大连化学物理研究所 | Method for synthesizing aviation kerosene cycloparaffin and arene by using waste polycarbonate plastic |
| CN115073253A (en) * | 2021-03-15 | 2022-09-20 | 中国科学院大连化学物理研究所 | Method for synthesizing dicycloalkane by polycarbonate plastic in one step |
| CN115073253B (en) * | 2021-03-15 | 2023-08-04 | 中国科学院大连化学物理研究所 | Method for synthesizing bicycloalkane by polycarbonate plastic in one step |
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