A method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure

Abstract

This invention discloses a method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure, belonging to the field of organic waste recycling. The method uses waste plastics, waste rubber, and waste oils as raw materials, employing a vertically connected two-stage reactor. Multiple types of mixed organic waste are co-pyrolyzed in the first-stage reactor, and the pyrolysis volatilization products directly enter the second-stage reactor for gaseous catalytic hydrogenation, ultimately yielding a mixed aviation liquid fuel containing different functional components. This method utilizes the molecular structure of organic waste itself to prepare liquid fuel products such as isoalkanes and aromatics, replacing the isomerization and aromatization reactions in existing catalytic processes. It has advantages such as a simple process flow and simple catalytic reaction, and can quantitatively prepare mixed aviation fuel composed of two or more functional components from n-alkanes, isoalkanes, aromatics, and cycloalkanes according to actual applications.

Description

Technical Field

[0001] This invention belongs to the field of organic waste recycling technology, specifically relating to a method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure. Background Technology

[0002] The global dual-carbon target has accelerated the transition from fossil fuels to renewable green energy. Against this backdrop, organic waste, potentially recyclable for producing green fuels, is increasingly attracting attention. Organic waste refers to organic items and substances generated during production, daily life, and other activities that have lost their original value and are discarded, such as waste plastics, waste rubber, and waste oils. Due to their large quantity, high C and H content, and high calorific value, organic waste has significant energy utilization value. It is estimated that the global annual production of waste oil exceeds 190 million tons, plastics approximately 380 million tons, and rubber approximately 29 million tons. This massive amount of organic waste has become a global problem, urgently requiring its rational disposal and reuse; however, the current situation regarding organic waste management is far from optimistic. Waste oil is mainly disposed of through landfills and sewer systems; waste rubber is primarily treated through incineration and landfill, with a recycling rate of approximately 30%; statistics on waste plastics are more precise: 27%-30% of plastics are littered or improperly disposed of, 2%-5% end up in the ocean, 40% are landfilled, 14% are burned for energy recovery, and only 14% are sorted and recycled for new product production. Landfilling causes irreversible damage to the soil, incineration exacerbates global warming, and all plastics leaked on land eventually drift into the ocean, where they slowly degrade into microplastics, severely impacting biodiversity. This demonstrates that current methods of organic waste disposal not only cause significant environmental damage but also result in substantial resource waste. In today's world, with fossil fuels increasingly depleted and the pursuit of carbon neutrality, converting organic waste into liquid fuels is of paramount importance.

[0003] Because oils and fats have similar chemical structures to liquid fuels, they are often used to produce liquid fuels. Currently, there are two main methods for converting oils and fats into liquid fuels: catalytic cracking and high-pressure hydrogenation. However, liquid fuels obtained from oils and fats through single catalytic cracking have a complex composition and still contain oxygen-containing compounds, resulting in low calorific value and unstable storage. Similarly, liquid fuels obtained from oils and fats through single high-pressure hydrogenation are generally only n-alkanes. However, currently used liquid fuels (gasoline, aviation fuel, and diesel) are mainly composed of multiple components such as n-alkanes, isoalkanes, aromatics, and cycloalkanes, so a single component cannot meet the various performance requirements of the fuel. For example, aromatics can improve the lubricity of fuel oil, cycloalkanes can increase the density and flash point of fuel oil, n-alkanes can increase the calorific value of fuel oil, and isoalkanes can improve the low-temperature fluidity of fuel oil. In order to obtain multi-component mixed liquid fuels, a series of catalytic steps have been carried out on the basis of traditional oil and fat conversion, mainly including two methods: catalytic cracking-aromatization-hydrogenation and high-pressure hydrogenation-hydrocracking / hydroisomerization. Invention patent CN 110257098 A discloses a method for preparing bio-aviation fuel and biodiesel by reducing the activation energy of the thermochemical conversion of bio-oils. This method involves catalytic cracking, aromatization, hydrogenation, and distillation of bio-oils to obtain bio-aviation fuel with a carbon chain length of C8-C15 and biodiesel with a carbon chain length of C16-C24. The oil is then processed through cracking catalysts, aromatization catalysts, and hydrogenation catalysts to ultimately obtain a biofuel consisting of a mixture of alkanes, cycloalkanes, and aromatics. However, to obtain the mixed fuel oil, this process requires three catalytic steps (deoxygenation / aromatization / hydrogenation saturation), making the process cumbersome and difficult to control the content of each component in the final product. Invention patent CN 109294613 B discloses a method for preparing hydrocarbon fuels from oil-based feedstocks. This method first performs a catalytic hydrogenation reaction on the oil to obtain n-alkanes, and then performs an isomerization reaction on the n-alkanes to obtain a mixed fuel of n-alkanes and isoalkanes. However, this process is carried out under high pressure (>1MPa) and requires organic solvents to dissolve the oils to increase the fluidity of the reaction system. It has disadvantages such as harsh process conditions, easy deactivation of catalysts, complicated reaction steps, and difficulty in controlling the content of mixed components. In addition, two catalysts are required to work together (hydrodeoxygenation / hydroisomerization) to obtain fuel with a mixture of two components.

[0004] Similarly, there are currently two main methods for producing blended liquid fuels from plastics. For plastics without benzene rings, the main method involves multi-step catalytic processes, including catalytic cracking and catalytic upgrading (isomerization / aromatization). Patent CN107746722A discloses a method and apparatus for producing gasoline and diesel from waste plastics through thermal cracking, catalytic cracking, and catalytic upgrading. For benzene-based oxygen-containing plastics, the main method involves mixing with a solvent, then subjecting the plastic to a hydrodeoxygenation reaction with a catalyst to break the chain, followed by hydrodeoxygenation / hydrogen saturation to obtain aromatics and cycloalkanes. Patent CN114181726A discloses a method for synthesizing aviation kerosene cycloalkanes and aromatics from waste polycarbonate plastics. This method involves mixing the plastic with an alcohol solvent, then subjecting the plastic to alcoholysis and hydrodeoxygenation reactions in the presence of a catalyst to break the long chains, followed by further hydrogenation to obtain aromatics and cycloalkanes. However, these methods generally involve liquid catalytic hydrogenation reactions in solvents, making the catalyst highly susceptible to deactivation and the composition of the product components difficult to control.

[0005] Waste rubber is mainly used to obtain mixed liquid fuels through catalytic pyrolysis. Invention patent CN 104560099 B discloses a process for producing fuel oil from waste rubber. This method involves mixing waste rubber with a catalyst and then performing catalytic pyrolysis to obtain mixed liquid fuel. However, this product still contains a large amount of unsaturated olefins, making the fuel extremely unstable.

[0006] To comprehensively utilize organic waste, existing research includes methods for preparing mixed liquid fuels through the co-pyrolysis of waste plastics, waste rubber, and waste oils. Invention patents CN 105038834 B and CN 104449831 A describe the thermal / catalytic cracking of waste oils and waste plastics to produce fuel oil; invention patent CN 104650940 A describes the catalytic cracking of waste rubber and waste plastics to produce fuel oil; and invention patent CN 105462603 A describes the catalytic cracking of waste plastics, waste rubber, and waste oil to produce fuel oil. However, fuel oil prepared solely through the catalytic cracking of organic waste contains a large amount of unsaturated olefins. These unstable components easily form gums, damaging machinery. Furthermore, the complex composition and difficult-to-control component content of the fuel oil result in poor fuel quality, making it unsuitable for practical applications.

[0007] In summary, existing processes for preparing blended liquid fuels from organic waste can be broadly categorized into two types based on the objects being converted: single-factor conversion and post-conversion conversion. For single-factor conversion, waste oils primarily consist of long-chain oxygen-containing structures, requiring hydrodeoxygenation-isomerization or catalytic cracking-aromatization (often containing unsaturated olefins) to obtain blended fuels with different molecular structures. Similarly, plastics without benzene rings can be pyrolyzed to obtain large-chain molecular structures, requiring isomerization / aromatization to obtain blended fuels with different molecular structures. Benzene-based oxygen-containing plastics require multi-step hydrodeoxygenation / hydrogenation reactions in solvents to obtain fuels containing a mixture of aromatics and cycloalkanes. Waste rubber is converted into liquid fuels containing a large amount of unsaturated olefins through catalytic cracking. For post-conversion conversion of different types of organic waste, direct catalytic cracking is the primary method, and the product is also fuel oil containing a large amount of unsaturated olefins. Therefore, existing processes for producing blended liquid fuels from organic waste require multiple complex catalytic reaction steps (cracking / isomerization / aromatization / hydrogenation / hydrodeoxygenation) to obtain high-quality blended liquid fuels. Furthermore, the degree of reaction in each catalytic step is difficult to control, resulting in uncontrollable content of blended fuel components. Simple catalytic reactions (thermal cracking / catalytic cracking) of blended organic waste can only yield poor-quality blended fuel oils (containing large amounts of unsaturated olefins), requiring further multiple catalytic steps to obtain high-quality blended liquid fuels. Summary of the Invention

[0008] To address the aforementioned problems in existing technologies, the technical problem this invention aims to solve is to provide a method for preparing aviation fuels with different functional components based on the directional dismantling of organic waste molecular structures. This method utilizes the molecular structure of organic waste itself to replace the isomerization and aromatization reactions in existing catalytic processes. Through a single catalytic reaction, high-quality mixed aviation fuels containing different functional components and meeting practical application requirements can be quantitatively prepared. This method has advantages such as a simple process flow and straightforward catalytic reaction. It solves the problems of existing processes, including cumbersome and complex catalytic processes, multiple catalytic reactions (cracking / isomerization / aromatization / hydrogenation / hydrodeoxygenation) making it difficult to control fuel oil component content, complex product composition (containing many unsaturated olefins) resulting in poor fuel oil quality, and harsh reaction conditions.

[0009] To solve the above-mentioned technical problems, the technical solution adopted by the present invention is as follows:

[0010] A method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure employs a vertically connected two-stage fixed-bed reactor. In the first-stage reactor, a mixture of organic waste is co-pyrolyzed, and in the second-stage reactor, the co-pyrolysis volatilization products are catalytically hydrogenated to obtain a mixed liquid aviation fuel composed of different functional components. The reaction temperature in the first-stage reactor is 480-550℃, and the reaction temperature in the second-stage reactor is 250-400℃. The reaction pressure in the two-stage reactor is 1-20 bar. The hydrogenation catalyst used for the catalytic hydrogenation reaction is any one of 1.5% Pd / SBA-15 (1.5% refers to the Pd loading rate), Ni / NiAl2O4, 30% Ni / Al2O3-SiO2 (30% refers to the Ni loading rate), 10% Pd / C (10% refers to the Pd loading rate), 10% Pt / C (10% refers to the Pt loading rate), or 10% Ru / C (10% refers to the Ru loading rate). Preferably, the organic waste is waste plastic, waste rubber, and waste oil; preferably, the waste plastic is any one of waste polystyrene (PS) plastic, waste polypropylene (PP) plastic, waste polycarbonate (PC) plastic, waste high-density polyethylene (HDPE) plastic, waste low-density polyethylene (LDPE) plastic, waste linear low-density polyethylene (LLDPE) plastic, waste polyethylene terephthalate (PET) plastic, waste high-impact polystyrene (HIPS) plastic, waste acrylonitrile-butadiene-styrene copolymer (ABS), or waste acrylonitrile-styrene copolymer (AS); the waste oil is any one of palm kernel oil, kitchen waste oil, bark oil, soybean oil, or coconut oil.

[0011] The method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure, wherein the organic waste mixture is waste polystyrene plastic and waste oil, and the hydrogenation catalyst is 1.5% Pd / SBA-15, the liquid product is a mixed aviation fuel composed of aromatic and n-alkane functional components.

[0012] The method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure uses waste acrylonitrile-styrene copolymer and waste oil as the organic waste mixture. When the hydrogenation catalyst is 10% Pd / C, the liquid product is a mixed aviation fuel composed of cycloalkanes and n-alkanes as functional components.

[0013] The method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure, wherein the organic waste mixture is waste polyethylene plastic and waste polypropylene plastic, and the hydrogenation catalyst is Ni / NiAl2O4, the liquid product is a mixed aviation fuel composed of n-alkanes and isoalkanes as functional components.

[0014] The method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure, wherein the organic waste mixture is waste natural rubber and waste polypropylene plastic, and the hydrogenation catalyst is 30% Ni / Al2O3-SiO2, the liquid product is a mixed aviation fuel composed of cycloalkanes and isoalkanes as functional components.

[0015] The method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure uses waste polycarbonate plastic and waste oil as the organic waste mixture. When the hydrogenation catalyst is 30% Ni / Al2O3-SiO2, the liquid product is a mixed aviation fuel composed of cycloalkanes, aromatics and n-alkanes as functional components.

[0016] The method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure uses waste natural rubber, waste polypropylene plastic and waste oil as the organic waste mixture. When the hydrogenation catalyst is 10% Ru / C, the liquid product is a mixed aviation fuel composed of cycloalkanes, isoalkanes and n-alkanes as functional components.

[0017] The method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure, wherein the organic waste mixture is waste polycarbonate plastic, waste polypropylene plastic and waste oil, and the hydrogenation catalyst is Ni / NiAl2O4, the liquid product is a mixed aviation fuel composed of functional components of aromatics, cycloalkanes, isoalkanes and n-alkanes.

[0018] Compared with the prior art, the beneficial effects of the present invention are as follows:

[0019] (1) This invention utilizes the molecular structure of organic waste to prepare liquid fuel products such as isoalkanes and aromatics, replacing the isomerization and aromatization reactions in the existing catalytic process. For example, waste polypropylene (PP) plastic can provide isoalkanes, waste oil can provide n-alkanes, waste polystyrene (PS) plastic can provide aromatics / cycloalkanes, and waste natural rubber can provide cycloalkanes / isoalkanes. Through the effect of the molecular structure of organic waste, high-quality mixed liquid aviation fuel can be obtained with just a simple one-step catalytic reaction, solving the problem of the cumbersome and complicated catalytic process (cracking / isomerization / aromatization / hydrogenation / hydrodeoxygenation) in the existing process.

[0020] (2) The present invention obtains gaseous intermediates containing unsaturated olefins and oxygen-containing compounds by co-pyrolysis of mixed organic waste. These gaseous intermediates can be further hydrogenated on a hydrogenation catalyst to obtain a completely deoxygenated mixed liquid aviation fuel without olefins. This solves the problems of liquid fuels obtained by existing processes being rich in unsaturated olefins, having complex components, and having poor fuel quality. It has the advantages of mild reaction conditions, simple process flow, low hydrogen consumption, and good fuel quality.

[0021] (3) This invention can quantitatively control the composition and content of each component of the blended fuel oil by designing the type and amount of organic waste added, and can also control it by changing conditions such as reaction temperature, reaction pressure and catalyst type. It can quantitatively prepare blended aviation fuel composed of two or more functional components from n-alkanes, isoalkanes, aromatics and cycloalkanes according to actual applications. Detailed Implementation

[0022] The present invention will be further described below with reference to specific embodiments.

[0023] Example 1

[0024] A method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure includes the following steps:

[0025] (1) 5 mg of 1.5% Pd / SBA-15 catalyst was loaded into a quartz tube and the quartz tube was filled into the secondary reactor; 0.3 mg of waste PS plastic and 0.7 mg of waste palm kernel oil were mixed and loaded into a sample bottle and the sample bottle was filled into the injection port; then, carrier helium gas was introduced at a flow rate of 100 ml / min through the sample loading port to purge the primary and secondary reactors in the series two-stage reactor for 5 min;

[0026] (2) Switch helium to hydrogen and purge the first and second stage reactors in the series two-stage reactor for 10 minutes. Then set the temperature of the first stage reactor to 490℃, the temperature of the second stage reactor to 360℃, and the reaction pressure to 1.5 bar via computer. At this time, the reactor begins to heat up and pressurize.

[0027] (3) After observing that the reactor temperature and pressure have stabilized to the set value and the gas chromatography-mass spectrometer has entered the working state, the sample bottle containing waste PS plastic and waste palm kernel oil is sent into the first-stage reactor for hydrogenation pyrolysis. The pyrolysis volatile products enter the second-stage reactor for hydrogenation reaction on a 1.5% Pd / SBA-15 catalyst. After the reaction is completed, the product is sent to the separation device, passes through the separation column, and enters the gas chromatography-mass spectrometer for online analysis. The results are shown in Table 1.

[0028] As shown in Table 1, the mixed aviation fuel obtained by co-pyrolysis of waste PS plastic and waste palm kernel oil and subsequent gaseous catalytic hydrogenation under the catalysis of 1.5% Pd / SBA-15 catalyst contains n-alkanes and aromatics, with a total yield of 84.4%; among which, the yield of n-alkanes is 56.2% and the yield of aromatics is 28.2%.

[0029] Example 2

[0030] A method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure includes the following steps:

[0031] (1) The catalyst used in this example is the catalyst that was not removed from the secondary reactor after the reaction in Example 1; 0.3 mg of waste PS plastic and 0.7 mg of waste palm kernel oil were mixed and put into a sample bottle, and the sample bottle was filled into the injection port; then the carrier gas helium was introduced and purged the first-stage reactor and the second-stage reactor in the series two-stage reactor at a flow rate of 120 ml / min through the sample filling point for 4 min;

[0032] (2) Switch helium to hydrogen and purge the first and second stage reactors in the series two-stage reactor to the end. Then set the temperature of the first stage reactor to 530°C, the temperature of the second stage reactor to 360°C, and the reaction pressure to 1.5 bar via computer. At this time, the reactor begins to heat up and pressurize.

[0033] (3) After observing that the reactor temperature and pressure have stabilized to the set value and the gas chromatography-mass spectrometer has entered the working state, the sample bottle containing waste PS plastic and waste palm kernel oil is sent into the first-stage reactor for hydrogenation pyrolysis. The pyrolysis volatilization products enter the second-stage reactor for hydrogenation reaction on a 1.5% Pd / SBA-15 catalyst. After the reaction is completed, the product is sent to the separation device, passes through the separation column, and enters the gas chromatography-mass spectrometer for online analysis. The results are shown in Table 1.

[0034] As shown in Table 1, the mixed aviation fuel obtained by co-pyrolysis of waste PS plastic and waste palm kernel oil under the catalysis of 1.5% Pd / SBA-15 catalyst and subsequent gaseous catalytic hydrogenation contains n-alkanes and aromatics, with a total yield of 73.1%; among which, the yield of n-alkanes is 44.4% and the yield of aromatics is 28.7%.

[0035] Example 3

[0036] A method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure includes the following steps:

[0037] (1) The catalyst used in this example is the catalyst that was not removed from the secondary reactor after the reaction in Example 2; 0.3 mg of waste PS plastic and 0.7 mg of waste palm kernel oil were mixed and put into a sample bottle, and the sample bottle was filled into the injection port; then the carrier gas helium was introduced and purged the first-stage reactor and the second-stage reactor in the series two-stage reactor at a flow rate of 140 ml / min through the sample filling point for 7 min;

[0038] (2) Switch helium to hydrogen and purge the first and second stage reactors in the series two-stage reactor for 15 minutes. Then set the temperature of the first stage reactor to 490℃, the temperature of the second stage reactor to 390℃, and the reaction pressure to 1.5 bar via computer. At this time, the reactor begins to heat up and pressurize.

[0039] (3) After observing that the reactor temperature and pressure have stabilized to the set value and the gas chromatography-mass spectrometer has entered the working state, the sample bottle containing waste PS plastic and waste palm kernel oil is sent into the first-stage reactor for hydrogenation pyrolysis. The pyrolysis volatilization products enter the second-stage reactor for hydrogenation reaction on a 1.5% Pd / SBA-15 catalyst. After the reaction is completed, the product is sent to the separation device, passes through the separation column, and enters the gas chromatography-mass spectrometer for online analysis. The results are shown in Table 1.

[0040] As shown in Table 1, the mixed aviation fuel obtained by co-pyrolysis of waste PS plastic and waste palm kernel oil under the catalysis of 1.5% Pd / SBA-15 catalyst and subsequent gaseous catalytic hydrogenation contains n-alkanes and aromatics, with a total yield of 68.5%; among which, the yield of n-alkanes is 43.7% and the yield of aromatics is 24.8%.

[0041] Example 4

[0042] A method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure includes the following steps:

[0043] (1) The catalyst used in this example is the catalyst that was not removed from the secondary reactor after the reaction in Example 3; 0.3 mg of waste HIPS plastic and 0.7 mg of waste palm kernel oil were mixed and put into a sample bottle, and the sample bottle was filled into the injection port; then the carrier gas helium was introduced and purged the first-stage reactor and the second-stage reactor in the series two-stage reactor at a flow rate of 130 ml / min through the sample filling point for 4 min;

[0044] (2) Switch helium to hydrogen and purge the first and second stage reactors in the series two-stage reactor for 11 minutes. Then set the temperature of the first stage reactor to 490℃, the temperature of the second stage reactor to 360℃, and the reaction pressure to 1.5 bar via computer. At this time, the reactor begins to heat up and pressurize.

[0045] (3) After observing that the reactor temperature and pressure have stabilized to the set value and the gas chromatography-mass spectrometer has entered the working state, the sample bottle containing waste HIPS plastic and waste palm kernel oil is sent into the first-stage reactor for hydrogenation pyrolysis. The pyrolysis volatile products enter the second-stage reactor for hydrogenation reaction on a 1.5% Pd / SBA-15 catalyst. After the reaction is completed, the product is sent to the separation device, passes through the separation column, and enters the gas chromatography-mass spectrometer for online analysis. The results are shown in Table 1.

[0046] As shown in Table 1, the mixed aviation fuel obtained by co-pyrolysis of waste HIPS plastic and waste palm kernel oil and subsequent gaseous catalytic hydrogenation under the catalysis of 1.5% Pd / SBA-15 catalyst contains n-alkanes and aromatics, with a total yield of 67.8%; among which, the yield of n-alkanes is 47.2% and the yield of aromatics is 20.6%.

[0047] Example 5

[0048] A method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure includes the following steps:

[0049] (1) The catalyst used in this example is the catalyst that was not removed from the secondary reactor after the reaction in Example 4; 0.3 mg of waste PS plastic and 0.7 mg of kitchen waste oil were mixed and put into a sample bottle, and the sample bottle was filled into the injection port; then the carrier gas helium was introduced and purged the first-stage reactor and the second-stage reactor in the series two-stage reactor at a flow rate of 120 ml / min through the sample filling point for 5 min;

[0050] (2) Switch helium to hydrogen and purge the first and second stage reactors in the series two-stage reactor for 10 minutes. Then set the temperature of the first stage reactor to 490℃, the temperature of the second stage reactor to 360℃, and the reaction pressure to 1.5 bar via computer. At this time, the reactor begins to heat up and pressurize.

[0051] (3) After observing that the reactor temperature and pressure have stabilized to the set value and the gas chromatography-mass spectrometry has entered the working state, the sample bottle containing waste PS plastic and kitchen waste oil is sent into the first-stage reactor for hydrogenation pyrolysis. The pyrolysis volatilization products enter the second-stage reactor for hydrogenation reaction on a 1.5% Pd / SBA-15 catalyst. After the reaction is completed, the product is sent to the separation device, passes through the separation column, and enters the gas chromatography-mass spectrometer for online analysis. The results are shown in Table 1.

[0052] As shown in Table 1, the mixed aviation fuel obtained by co-pyrolysis of waste PS plastic and kitchen waste oil under the catalysis of 1.5% Pd / SBA-15 catalyst and subsequent gaseous catalytic hydrogenation contains n-alkanes and aromatics, with a total yield of 81.7%; among which, the yield of n-alkanes is 59.6% and the yield of aromatics is 22.1%.

[0053] Example 6

[0054] A method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure includes the following steps:

[0055] (1) The catalyst used in this example is the catalyst that was not removed from the secondary reactor after the reaction in Example 5; 0.3 mg of waste PS plastic and 0.7 mg of waste scleroderma oil were mixed and put into a sample bottle, and the sample bottle was filled into the injection port; then, carrier helium gas was introduced and purged the first-stage and second-stage reactors in the series two-stage reactors at a flow rate of 130 ml / min through the sample filling point for 5 min;

[0056] (2) Switch helium to hydrogen and purge the first and second stage reactors in the series two-stage reactor for 13 minutes. Then set the temperature of the first stage reactor to 490℃, the temperature of the second stage reactor to 360℃, and the reaction pressure to 1.5 bar via computer. At this time, the reactor begins to heat up and pressurize.

[0057] (3) After observing that the reactor temperature and pressure have stabilized to the set value and the gas chromatography-mass spectrometer has entered the working state, the sample bottle containing waste PS plastic and waste scleroderma oil is sent into the first-stage reactor for hydrogenation pyrolysis. The pyrolysis volatilization products enter the second-stage reactor for hydrogenation reaction on a 1.5% Pd / SBA-15 catalyst. After the reaction is completed, the product is sent to the separation device, passes through the separation column, and enters the gas chromatography-mass spectrometer for online analysis. The results are shown in Table 1.

[0058] As shown in Table 1, the mixed aviation fuel obtained by co-pyrolysis of waste PS plastic and waste scleroderma oil under the catalysis of 1.5% Pd / SBA-15 catalyst and subsequent gaseous catalytic hydrogenation contains n-alkanes and aromatics, with a total yield of 74.3%; among which, the yield of n-alkanes is 52.5% and the yield of aromatics is 21.8%.

[0059] Example 7

[0060] A method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure includes the following steps:

[0061] (1) 6 mg of 30% Ni / Al2O3-SiO2 catalyst was loaded into a quartz tube and then the quartz tube was filled into the secondary reactor; 1.4 mg of waste natural rubber and 0.6 mg of waste PP plastic were mixed and loaded into a sample bottle and then the sample bottle was filled into the inlet; then carrier helium gas was introduced at a flow rate of 120 ml / min through the sample loading point to purge the primary and secondary reactors in the series two-stage reactor for 5 min;

[0062] (2) Switch helium to hydrogen and purge the first and second stage reactors in the series two-stage reactor for 10 minutes. Then set the temperature of the first stage reactor to 480℃, the temperature of the second stage reactor to 250℃, and the reaction pressure to 2 bar via computer. At this time, the reactor begins to heat up and pressurize.

[0063] (3) After observing that the reactor temperature and pressure have stabilized to the set value and the gas chromatography-mass spectrometer has entered the working state, the sample bottle containing waste natural rubber and waste PP plastic is sent into the primary reactor for hydrogenation pyrolysis. The pyrolysis volatilization products enter the secondary reactor for hydrogenation reaction on a 30% Ni / Al2O3-SiO2 catalyst. After the reaction is completed, the product is sent to the separation device, passes through the separation column, and enters the gas chromatography-mass spectrometer for online analysis. The results are shown in Table 2.

[0064] As shown in Table 2, the mixed aviation fuel obtained by co-pyrolysis of waste natural rubber and waste PP plastic under the catalysis of 30% Ni / Al2O3-SiO2 catalyst and subsequent gaseous catalytic hydrogenation contains cycloalkanes and isoalkanes, with a total yield of 75.9%; among which, the yield of cycloalkanes is 40.6% and the yield of isoalkanes is 35.3%.

[0065] Example 8

[0066] A method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure includes the following steps:

[0067] (1) 6 mg of 10% Ru / C catalyst was loaded into a quartz tube and then the quartz tube was filled into the secondary reactor; 1.0 mg of waste natural rubber, 0.4 mg of waste PP plastic and 0.6 mg of waste palm kernel oil were mixed and then loaded into a sample bottle and then the sample bottle was filled into the injection port; then carrier gas helium was introduced and purged the primary and secondary reactors in the series two-stage reactors at a flow rate of 130 ml / min through the sample loading port for 5 min;

[0068] (2) Switch helium to hydrogen and purge the first and second stage reactors in the series two-stage reactor for 13 minutes. Then set the temperature of the first stage reactor to 480℃, the temperature of the second stage reactor to 250℃, and the reaction pressure to 2 bar via computer. At this time, the reactor begins to heat up and pressurize.

[0069] (3) After observing that the reactor temperature and pressure have stabilized to the set value and the gas chromatography-mass spectrometer has entered the working state, the sample bottle containing waste natural rubber, waste PP plastic and waste palm kernel oil is sent into the first-stage reactor for hydrogenation pyrolysis. The pyrolysis volatilization products enter the second-stage reactor for hydrogenation reaction on a 10% Ru / C catalyst. After the reaction is completed, the product is sent to the separation device, passes through the separation column and enters the gas chromatography-mass spectrometer for online analysis. The results are shown in Table 2.

[0070] As shown in Table 2, under the catalysis of a 10% Ru / C catalyst, the mixed aviation fuel obtained by co-pyrolysis of waste natural rubber, waste PP plastic, and waste palm kernel oil, followed by gaseous catalytic hydrogenation, contains cycloalkanes, isoalkanes, and n-alkanes, with a total yield of 79.9%; among which, the yield of cycloalkanes is 32.2%, the yield of isoalkanes is 22.6%, and the yield of n-alkanes is 25.1%.

[0071] Example 9

[0072] A method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure includes the following steps:

[0073] (1) 5 mg of 10% Pt / C catalyst was loaded into a quartz tube and the quartz tube was filled into the secondary reactor; 1 mg of waste PS plastic and 2 mg of waste palm kernel oil were mixed and loaded into a sample bottle and the sample bottle was filled into the injection port; then carrier helium gas was introduced at a flow rate of 150 ml / min through the sample loading port to purge the primary and secondary reactors in the series two-stage reactor for 4 min;

[0074] (2) Switch helium to hydrogen and purge the first and second stage reactors in the series two-stage reactor for 10 minutes. Then set the temperature of the first stage reactor to 480℃, the temperature of the second stage reactor to 260℃, and the reaction pressure to 4 bar via computer. At this time, the reactor begins to heat up and pressurize.

[0075] (3) After observing that the reactor temperature and pressure have stabilized to the set value and the gas chromatography-mass spectrometer has entered the working state, the sample bottle containing waste PS plastic and waste palm kernel oil is sent into the first-stage reactor for hydrogenation pyrolysis. The pyrolysis volatilization products enter the second-stage reactor for hydrogenation reaction on a 10% Pt / C catalyst. After the reaction is completed, the product is sent to the separation device, passes through the separation column, and enters the gas chromatography-mass spectrometer for online analysis. The results are shown in Table 2.

[0076] As shown in Table 2, under the catalysis of 10% Pt / C catalyst, the mixed aviation fuel obtained by co-pyrolysis of waste PS plastic and waste palm kernel oil, followed by gaseous catalytic hydrogenation, contains n-alkanes and cycloalkanes, with a total yield of 83.0%; among which, the yield of n-alkanes is 53.3% and the yield of cycloalkanes is 29.7%.

[0077] Example 10

[0078] A method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure includes the following steps:

[0079] (1) 5 mg of 10% Pd / C catalyst was loaded into a quartz tube and the quartz tube was then loaded into the secondary reactor; 1 mg of waste AS plastic and 2 mg of waste palm kernel oil were mixed and loaded into a sample bottle and the sample bottle was then loaded into the inlet; then carrier helium gas was introduced at a flow rate of 80 ml / min through the sample loading point to purge the primary and secondary reactors in the series two-stage reactor for 7 min;

[0080] (2) Switch helium to hydrogen and purge the first and second stage reactors in the series two-stage reactor for 15 minutes. Then set the temperature of the first stage reactor to 480℃, the temperature of the second stage reactor to 260℃, and the reaction pressure to 4 bar via computer. At this time, the reactor begins to heat up and pressurize.

[0081] (3) After observing that the reactor temperature and pressure have stabilized to the set value and the gas chromatography-mass spectrometer has entered the working state, the sample bottle containing waste AS plastic and waste palm kernel oil is sent into the first-stage reactor for hydrogenation pyrolysis. The pyrolysis volatilization products enter the second-stage reactor for hydrogenation reaction on a 10% Pd / C catalyst. After the reaction is completed, the product is sent to the separation device, passes through the separation column, and enters the gas chromatography-mass spectrometer for online analysis. The results are shown in Table 2.

[0082] As shown in Table 2, under the catalysis of 10% Pd / C catalyst, the mixed aviation fuel obtained by co-pyrolysis of waste AS plastic and waste palm kernel oil and subsequent gaseous catalytic hydrogenation contains n-alkanes and cycloalkanes, with a total yield of 77.9%; among which, the yield of n-alkanes is 50.9% and the yield of cycloalkanes is 27.0%.

[0083] Example 11

[0084] A method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure includes the following steps:

[0085] (1) 5 mg of 30% Ni / Al2O3-SiO2 catalyst was loaded into a quartz tube and then the quartz tube was filled into the secondary reactor; 0.5 mg of waste LLDPE plastic, 1 mg of waste PS plastic and 1.5 mg of waste soybean oil were mixed and loaded into a sample bottle and then the sample bottle was filled into the inlet; then carrier helium gas was introduced at a flow rate of 120 ml / min through the sample loading point to purge the primary and secondary reactors in the series two-stage reactor for 5 min;

[0086] (2) Switch helium to hydrogen and purge the first and second stage reactors in the series two-stage reactor for 14 minutes. Then set the temperature of the first stage reactor to 480℃, the temperature of the second stage reactor to 260℃, and the reaction pressure to 4 bar via computer. At this time, the reactor begins to heat up and pressurize.

[0087] (3) After observing that the reactor temperature and pressure have stabilized to the set value and the gas chromatography-mass spectrometer has entered the working state, the sample bottle containing waste LLDPE plastic, waste PS plastic and waste soybean oil is sent into the first-stage reactor for hydrogenation pyrolysis. The pyrolysis volatilization products enter the second-stage reactor for hydrogenation reaction on a 30% Ni / Al2O3-SiO2 catalyst. After the reaction is completed, the product is sent to the separation device, passes through the separation column and enters the gas chromatography-mass spectrometer for online analysis. The results are shown in Table 2.

[0088] As shown in Table 2, under the catalysis of 30% Ni / Al2O3-SiO2 catalyst, the mixed aviation fuel obtained by co-pyrolysis of waste LLDPE plastic, waste PS plastic and waste soybean oil, and subsequent gaseous catalytic hydrogenation, contains n-alkanes and cycloalkanes, with a total yield of 79.1%; among which, the yield of n-alkanes is 48.8% and the yield of cycloalkanes is 30.3%.

[0089] Example 12

[0090] A method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure includes the following steps:

[0091] (1) The catalyst used in this example is the catalyst that was not removed from the secondary reactor after the reaction in Example 7; 0.8 mg of waste PC plastic and 1.2 mg of kitchen waste oil were mixed and put into a sample bottle, and the sample bottle was filled into the injection port; then the carrier gas helium was introduced and purged the first-stage reactor and the second-stage reactor in the series two-stage reactor at a flow rate of 130 ml / min through the sample filling point for 6 min;

[0092] (2) Switch helium to hydrogen and purge the first and second stage reactors in the series two-stage reactor for 11 minutes. Then set the temperature of the first stage reactor to 530℃, the temperature of the second stage reactor to 300℃, and the reaction pressure to 3.2 bar via computer. At this time, the reactor begins to heat up and pressurize.

[0093] (3) After observing that the reactor temperature and pressure have stabilized to the set value and the gas chromatography-mass spectrometer has entered the working state, the sample bottle containing waste PC plastic and kitchen waste oil is sent into the first-stage reactor for hydrogenation pyrolysis. The pyrolysis volatilization products enter the second-stage reactor for hydrogenation reaction on a 30% Ni / Al2O3-SiO2 catalyst. After the reaction is completed, the product is sent to the separation device, passes through the separation column, and enters the gas chromatography-mass spectrometer for online analysis. The results are shown in Table 3.

[0094] As shown in Table 3, under the catalysis of 30% Ni / Al2O3-SiO2 catalyst, the mixed aviation fuel obtained by co-pyrolysis of waste PC plastic and kitchen waste oil, followed by gaseous catalytic hydrogenation, contains n-alkanes, aromatics, and cycloalkanes, with a total yield of 79.8%; among which, the yield of n-alkanes is 50.1%, the yield of aromatics is 8.9%, and the yield of cycloalkanes is 20.8%.

[0095] Example 13

[0096] A method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure includes the following steps:

[0097] (1) The catalyst used in this example is the catalyst that was not removed from the secondary reactor after the reaction in Example 12; 0.8 mg of waste PET plastic and 1.2 mg of waste coconut oil were mixed and put into a sample bottle, and the sample bottle was filled into the injection port; then the carrier gas helium was introduced and purged the first-stage reactor and the second-stage reactor in the series two-stage reactor at a flow rate of 140 ml / min through the sample filling point for 6 min;

[0098] (2) Switch helium to hydrogen and purge the first and second stage reactors in the series two-stage reactor for 14 minutes. Then set the temperature of the first stage reactor to 530℃, the temperature of the second stage reactor to 300℃, and the reaction pressure to 3.2 bar via computer. At this time, the reactor begins to heat up and pressurize.

[0099] (3) After observing that the reactor temperature and pressure have stabilized to the set value and the gas chromatography-mass spectrometer has entered the working state, the sample bottle containing waste PET plastic and waste coconut oil is sent into the first-stage reactor for hydrogenation pyrolysis. The pyrolysis volatilization products enter the second-stage reactor for hydrogenation reaction on a 30% Ni / Al2O3-SiO2 catalyst. After the reaction is completed, the product is sent to the separation device, passes through the separation column, and enters the gas chromatography-mass spectrometer for online analysis. The results are shown in Table 1.

[0100] As shown in Table 3, the mixed aviation fuel obtained by co-pyrolysis of waste PET plastic and waste coconut oil under the catalysis of 30% Ni / Al2O3-SiO2 catalyst and subsequent gaseous catalytic hydrogenation contains n-alkanes and aromatics, with a total yield of 62.7%; among which, the yield of n-alkanes is 52.8% and the yield of aromatics is 9.9%.

[0101] Example 14

[0102] A method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure includes the following steps:

[0103] (1) 6 mg of Ni / NiAl2O4 catalyst was loaded into a quartz tube and then the quartz tube was filled into the secondary reactor; 0.8 mg of waste PP plastic and 1.2 mg of waste soybean oil were mixed and then loaded into a sample bottle and then the sample bottle was filled into the injection port; then carrier gas helium was introduced and purged the first-stage and second-stage reactors in the series two-stage reactors at a flow rate of 100 ml / min through the sample loading port for 6 min;

[0104] (2) Switch helium to hydrogen and purge the first and second stage reactors in the series two-stage reactor for 13 minutes. Then set the temperature of the first stage reactor to 530℃, the temperature of the second stage reactor to 300℃, and the reaction pressure to 3.2 bar via computer. At this time, the reactor begins to heat up and pressurize.

[0105] (3) After observing that the reactor temperature and pressure have stabilized to the set value and the gas chromatography-mass spectrometer has entered the working state, the sample bottle containing waste PP plastic and waste soybean oil is sent into the first-stage reactor for hydrogenation pyrolysis. The pyrolysis volatilization products enter the second-stage reactor for hydrogenation reaction on Ni / NiAl2O4 catalyst. After the reaction is completed, the product is sent to the separation device, passes through the separation column, and enters the gas chromatography-mass spectrometer for online analysis. The results are shown in Table 3.

[0106] As shown in Table 3, the mixed aviation fuel obtained by co-pyrolysis of waste PP plastic and waste soybean oil under the catalysis of Ni / NiAl2O4 catalyst and subsequent gaseous catalytic hydrogenation contains n-alkanes and isoalkanes, with a total yield of 80.4%; among which, the yield of n-alkanes is 49.8% and the yield of isoalkanes is 30.6%.

[0107] Example 15

[0108] A method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure includes the following steps:

[0109] (1) The catalyst used in this example is the catalyst that was not removed from the secondary reactor after the reaction in Example 14; 1.3 mg of waste LDPE plastic and 0.7 mg of waste PP plastic were mixed and put into a sample bottle, and the sample bottle was filled into the injection port; then the carrier gas helium was introduced and purged the first-stage reactor and the second-stage reactor in the series two-stage reactor at a flow rate of 100 ml / min through the sample filling point for 3 min;

[0110] (2) Switch helium to hydrogen and purge the first and second stage reactors in the series two-stage reactor for 15 minutes. Then set the temperature of the first stage reactor to 530°C, the temperature of the second stage reactor to 300°C, and the reaction pressure to 3.2 bar via computer. At this time, the reactor begins to heat up and pressurize.

[0111] (3) After observing that the reactor temperature and pressure have stabilized to the set value and the gas chromatography-mass spectrometer has entered the working state, the sample bottle containing waste HDPE plastic and waste PP plastic is sent into the first-stage reactor for hydrogenation pyrolysis. The pyrolysis volatilization products enter the second-stage reactor for hydrogenation reaction on Ni / NiAl2O4 catalyst. After the reaction is completed, the product is sent to the separation device, passes through the separation column, and enters the gas chromatography-mass spectrometer for online analysis. The results are shown in Table 3.

[0112] As shown in Table 3, the mixed aviation fuel obtained by co-pyrolysis of waste LDPE plastic and waste PP plastic under the catalysis of Ni / NiAl2O4 catalyst and subsequent gaseous catalytic hydrogenation contains n-alkanes and isoalkanes, with a total yield of 82.4%; among which, the yield of n-alkanes is 52.0% and the yield of isoalkanes is 30.4%.

[0113] Example 16

[0114] A method for preparing aviation fuel with different functional components based on the directional dismantling of organic waste molecular structure includes the following steps:

[0115] (1) The catalyst used in this example is the catalyst that was not removed from the secondary reactor after the reaction in Example 15; 0.5 mg of waste PP plastic, 0.5 mg of waste PC plastic and 1 mg of kitchen waste oil were mixed and put into a sample bottle, and the sample bottle was filled into the injection port; then the carrier gas helium was introduced and purged the first-stage reactor and the second-stage reactor in the series two-stage reactor at a flow rate of 130 ml / min through the sample filling point for 7 min;

[0116] (2) Switch helium to hydrogen and purge the first and second stage reactors in the series two-stage reactor for 10 minutes. Then set the temperature of the first stage reactor to 530℃, the temperature of the second stage reactor to 300℃, and the reaction pressure to 3.2 bar via computer. At this time, the reactor begins to heat up and pressurize.

[0117] (3) After observing that the reactor temperature and pressure have stabilized to the set value and the gas chromatography-mass spectrometer has entered the working state, the sample bottle containing waste PP plastic, waste PC plastic and kitchen waste oil is sent into the first-stage reactor for hydrogenation pyrolysis. The pyrolysis volatilization products enter the second-stage reactor for hydrogenation reaction on Ni / NiAl2O4 catalyst. After the reaction is completed, the product is sent to the separation device, passes through the separation column, and enters the gas chromatography-mass spectrometer for online analysis. The results are shown in Table 3.

[0118] As shown in Table 3, under the catalysis of Ni / NiAl2O4 catalyst, the mixed aviation fuel obtained by co-pyrolysis of waste PP plastic, waste PC plastic and kitchen waste oil, and subsequent gaseous catalytic hydrogenation, contains n-alkanes, isoalkanes, aromatics and cycloalkanes, with a total yield of 79.3%; among which, the yield of n-alkanes is 40.2%, the yield of isoalkanes is 18.4%, the yield of aromatics is 8.2%, and the yield of cycloalkanes is 12.5%.

[0119] Table 1. Experimental results of Examples 1-6

[0120]

[0121]

[0122] Table 2 Experimental Results of Examples 7-11

[0123]

[0124] Table 3 Experimental results of Examples 12-16

[0125]

[0126]

[0127] The formulas for calculating the yields of liquid products (aviation fuel), n-alkanes, isoalkanes, aromatics, and cycloalkanes in Table 1-3 are shown below:

[0128]

[0129]

[0130]

[0131]

[0132]

Claims

1. A method for preparing aviation fuel based on the directional dismantling of organic waste molecules, characterized in that, A vertically connected two-stage fixed-bed reactor is used. The organic waste mixture is co-pyrolyzed in the first-stage reactor, and the co-pyrolysis volatilization products are catalytically hydrogenated in the second-stage reactor to obtain a mixed liquid aviation fuel composed of different functional components. The reaction temperature of the first-stage reactor is 480-550℃, and the reaction temperature of the second-stage reactor is 250-400℃. The reaction pressure of the two-stage reactor is 1-20 bar. The organic waste mixture consists of waste natural rubber and waste polypropylene plastic, the hydrogenation catalyst is 30% Ni / Al2O3-SiO2, and the liquid product is a mixed aviation fuel composed of cycloalkanes and isoalkanes as functional components.

2. A method for preparing aviation fuel based on the directional dismantling of organic waste molecules, characterized in that, A vertically connected two-stage fixed-bed reactor is used. The organic waste mixture is co-pyrolyzed in the first-stage reactor, and the co-pyrolysis volatilization products are catalytically hydrogenated in the second-stage reactor to obtain a mixed liquid aviation fuel composed of different functional components. The reaction temperature of the first-stage reactor is 480-550℃, and the reaction temperature of the second-stage reactor is 250-400℃. The reaction pressure of the two-stage reactor is 1-20 bar. The organic waste mixture consists of waste natural rubber, waste polypropylene plastic and waste oil, the hydrogenation catalyst is 10% Ru / C, and the liquid product is a mixed aviation fuel composed of functional components of cycloalkanes, isoalkanes and n-alkanes.

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