CN105567285B - A method for simultaneously preparing long-chain alkanes and aromatics from waste oil - Google Patents

Abstract

The present invention relates to a kind of method for preparing long chain alkane and aromatic hydrocarbons simultaneously by raw material of gutter oil, comprise the following steps：1) after gutter oil and water are mixed, hydrolysis occurs for heating, and C is obtained through processing₈~C₁₈Aliphatic acid；2) by C₈~C₁₈Aliphatic acid and catalyst add high-temperature high-pressure reaction kettle together, are heated to 270~370 DEG C of 1~7h of decarboxylation aromatization；Described catalyst is Pt/C；3) reaction product is cooled down, and is dissolved with organic solvent, liquid product and solid-phase catalyst are obtained after filtering.The inventive method not additional any hydrogen source and solvent, obtain the long chain alkane and aromatic hydrocarbons of high yield from gutter oil, and the yield of long chain alkane and aromatic hydrocarbons can respectively reach 69.3% and more than 20.1%.

Description

A method for simultaneously preparing long-chain alkanes and aromatics from waste oil

technical field

The invention relates to the field of oil degradation, in particular to a method for simultaneously preparing long-chain alkanes and aromatics from waste oil.

Background technique

With the rapid development of the aviation industry, by 2050, the amount of carbon dioxide produced by aircraft will exceed the sum of emissions from vehicles on the ground, and with the shrinking of oil resources, the price of crude oil will inevitably rise, putting airlines under enormous pressure for survival. Under pressure, people are working hard to find alternatives to traditional fossil fuels. 85% of the cost of bio-jet fuel is raw material costs, so it is very important to find suitable raw materials. As the main raw material of jet fuel, its significance is even more significant.

Waste oil generally refers to all kinds of low-quality oils that exist in daily life, and its sources are kitchen waste, waste oil from low-quality animal processing, and tail oil repeatedly used in fried foods. Upgrading waste oil to high value-added bio-jet fuel can not only solve the problem of waste oil treatment in our country, but also greatly reduce the carbon emissions of the aviation industry, and realize the real transformation of waste into wealth. At present, the mainstream technology for producing bio-aviation oil from waste oil is to first hydrolyze it into fatty acids and then hydrodeoxygenate it to remove the O in the oil in the form of H ₂ O to obtain long-chain alkanes, and then the long-chain alkanes undergo isomerization Preparation of bio-fuel. However, the _H2 consumption of the hydrodeoxygenation method is relatively large. As a commonly used hydrogen source, _H2 has great safety and storage and transportation problems. Moreover, China mainly uses coal to produce hydrogen, and there are problems such as high energy consumption, serious pollution and high _CO2 emission intensity in the process of hydrogen production. Therefore, reducing hydrogen consumption is an urgent problem to be solved in the development of bio-aviation fuel in my country.

The decarboxylation method removes O in the form of CO ₂ , does not consume hydrogen in deoxygenation, and can effectively and greatly reduce hydrogen consumption. The H ₂ added in the reaction is only used to saturate the double bonds in oleic acid, which has reduced the consumption of H ₂ compared with hydrodeoxygenation, but still requires the addition of H ₂ , which does not fundamentally solve the problem.

The basic composition of aviation fuel is alkanes, cycloalkanes, aromatics and a small amount of additives with a carbon chain length between 8 and 17. Although alkanes have better combustion performance, the expansion function of the entire fuel elastic system must be realized by aromatics, so aromatics are also an essential component, but aromatics are difficult to obtain from mature hydrodeoxygenation technology or Fischer-Tropsch Synthetic obtained, generally come from straight-run kerosene. There are very few aromatics produced from biomass, and only some cracking methods can produce a small amount of aromatics, and the aromatics that can be produced are generally lignin and other biomass with low energy density, and most of the aromatics produced are polycyclic, which is not suitable for aviation fuel. requirements (Fuel, 2015.160: p.375-385). For the preparation of aromatics from fats and oils, although the yield of aromatics can reach 24%, the conditions are very harsh, the temperature is 800°C, the quality of the catalyst is 20 times that of biomass, and 24% of unknown residues remain. It can be seen that in this system, even the cracking of waste oil containing polyunsaturated bonds is difficult to obtain the key component aromatics of aviation fuel.

"Research on non-hydrogen-catalyzed decarboxylation of fatty acids (esters)" (Yang Cuiyue, China Excellent Master's Dissertation Full-text Database Engineering Science and Technology Series II) discloses a method of non-hydrogen-catalyzed decarboxylation of microalgal oils in high-temperature liquid water to prepare long-chain alkanes method, but this reaction does not produce aromatic hydrocarbons. It is precisely because of the presence of water in the decarboxylation reaction that the dehydrogenation of unsaturated acids and intermediate products is inhibited, so that the intramolecular D-A reaction aromatization cannot continue, resulting in no aromatic hydrocarbons in the final product.

Contents of the invention

The purpose of the present invention is to address the deficiencies in the prior art and provide a method for simultaneously preparing long-chain alkanes and aromatics from waste oil, which can not only solve the problem of waste oil in my country, but also greatly reduce the cost of preparing bio-aviation oil. Hydrogen consumption.

The technical scheme provided by the present invention is:

A method for simultaneously preparing long-chain alkanes and aromatics from waste oil as a raw material, comprising the steps of:

1) After the waste oil is mixed with water, it is heated to undergo a hydrolysis reaction, and C ₈ -C ₁₈ fatty acids are obtained after treatment;

2) Add C ₈ -C ₁₈ fatty acids and a catalyst into a high-temperature and high-pressure reactor, heat up to 270-370°C for decarboxylation and aromatization for 1-7 hours; the catalyst is Pt/C;

3) The reaction product is cooled, dissolved with an organic solvent, and filtered to obtain a liquid phase product and a solid phase catalyst.

In the present invention, gutter oil is prepared through a two-step method of non-catalyzed hydrolysis and non-hydrogen decarboxylation aromatization reaction to prepare long-chain alkanes and aromatics. The first step of hydrolysis does not require a catalyst, and the hydrolysis temperature is not high. The second step does not add any hydrogen. Hydrogen agent or solvent, using the catalysis of Pt/C to dehydrogenate a part of unsaturated fatty acids and their decarboxylation products and further intramolecular D-A reaction aromatization to supply hydrogen, the generated hydrogen quickly saturates the remaining unsaturated fatty acids into saturated fatty acids, Decarboxylation of saturated fatty acids to long-chain alkanes. Using Pt/C, the four processes of dehydrogenation, decarboxylation, hydrogenation, and aromatization can be coupled in one step without solvent and external hydrogen donor, and long-chain alkanes and aromatics can be obtained at the same time. The reaction process has zero hydrogen consumption, is simple and reliable.

The first step is non-catalytic hydrolysis of waste oil in near-critical water, and the glyceride in the raw material is hydrolyzed into free fatty acids, which contain saturated fatty acids and most unsaturated fatty acids; the second step is the unsaturated fatty acids in free fatty acids. Aromatization occurs under the action of a part to produce hydrogen, and the rest is hydrogenated to become saturated fatty acids, and finally all the saturated fatty acids are decarboxylated to become alkanes. The reaction equation is shown in Figure 1.

The main components of the C ₈ -C ₁₈ fatty acids obtained in step 1) are docosahexaenoic acid, stearic acid, palmitic acid, oleic acid, linoleic acid, linolenic acid, dodecanoic acid and the like.

In step 2), since the hydrolyzed products C ₈ -C ₁₈ contain saturated and unsaturated fatty acids, the decarboxylation reaction process is relatively complicated, so the decarboxylation reaction needs to select a suitable catalyst and reaction temperature and other reaction conditions.

The decarboxylation aromatization in step 2) is non-hydrodecarboxylation aromatization, and does not require any additional hydrogen, solvent or hydrogen donor.

The catalyst described in step 2) is Pt/C, and the catalytic effect is better. Without adding any hydrogen, hydrogen donor or solvent, a part of the unsaturated fatty acid and its decarboxylation product are dehydrogenated by the catalytic action of Pt/C and further molecular The internal D-A reaction aromatizes hydrogen, and the generated hydrogen quickly saturates the remaining unsaturated fatty acids into saturated fatty acids, and decarboxylates the saturated fatty acids to grow chain alkanes. Using Pt/C, it can be dehydrogenated in the state of no solvent and an external hydrogen donor. The four processes of decarboxylation, hydrogenation and aromatization are coupled in one step, and long-chain alkanes and aromatics are obtained at the same time. The reaction process has zero hydrogen consumption, is simple and reliable.

The organic solvent in the described step 3) can be acetone, n-hexane or dichloromethane etc.

Preferably, the mass ratio of waste oil to water in the step 1) is 1:0.5-5; the hydrolysis reaction temperature is 160-260°C. Due to the complex composition of waste oil, the hydrolysis reaction is relatively difficult, and increasing the temperature of the reaction system can accelerate the hydrolysis of waste oil. In this temperature range, the water becomes high-temperature liquid water, and the high-temperature liquid water has a certain acid-base catalytic ability, which can accelerate the hydrolysis speed of waste oil and increase the reaction yield.

As a further preference, the mass ratio of waste oil to water in step 1) is 1:3-5; under this condition, the hydrolysis reaction yield can reach more than 93%.

As a preference, the time for the hydrolysis reaction in the step 1) is 4-10 hours.

Preferably, the mass ratio of waste oil to catalyst in step 2) is 6-14:1.

As a further preference, the mass ratio of waste oil to catalyst in step 2) is 6.25˜10:1.

As an improvement, the solid-phase catalyst in step 3) continues to be cleaned and vacuum-dried. The solid-phase catalyst can be recycled and reused after being cleaned and dried to improve economic benefits.

As preferably, the mass ratio of waste oil and water in the step 1) is 1:4～5; the hydrolysis reaction temperature is 160～180°C; the mass ratio of waste oil and the catalyst in the step 2) is 6.25～ 7:1; In the step 2) described above, heat up to 350-370°C for decarboxylation and aromatization for 1-3 hours. Under the preferred conditions, the yield of long chain alkanes is greater than 67% and the yield of aromatics is greater than 19%.

Compared with the prior art, the beneficial effects of the present invention are reflected in:

(1) The waste oil output of the raw material of the present invention is large, and if it flows to the dining table again, it will seriously affect people's health. Therefore, it is an economical and promising method to prepare high-grade long-chain alkanes and aromatics with waste oil as raw material.

(2) Catalyst Pt/C of the present invention can make the unsaturated fatty acid in the waste oil hydrolyzate and its decarboxylation product become hydrogen donating agent, produce hydrogen by dehydroaromatization, without any hydrogen source and solvent, react The process does not consume hydrogen, saves energy, and is carried out under solvent-free conditions, reducing environmental pollution. The catalyst Pt/C has good stability, can be used repeatedly, and reduces the cost of catalysis.

(3) The method of the present invention does not add any hydrogen sources and solvents, and obtains high-yield long-chain alkanes from waste oil and aromatics, an important component of aviation fuel that is difficult to obtain through other hydrodeoxygenation or Fischer-Tropsch synthesis, and long-chain alkanes The yields of aromatics and aromatics can reach above 69.3% and 20.1% respectively.

Description of drawings

Fig. 1 is the reaction equation of preparing long-chain alkanes and aromatics simultaneously with waste oil as raw material;

Fig. 2 is a flow chart of a method for simultaneously preparing long-chain alkanes and aromatics from waste oil.

detailed description

In the following examples, waste oil is used as raw material, and non-catalyzed hydrolysis in near-critical water yields hydrolyzed products that are separated to obtain C ₈ -C ₁₈ saturated and unsaturated fatty acids; since there is no external hydrogen source, a part of waste oil hydrolyzed products C ₈ - C ₁₈ unsaturated fatty acids are dehydrogenated under the action of catalyst Pt/C to become polyolefins, polyolefins are aromatized into aromatic hydrocarbons, and the remaining unsaturated fatty acids are hydrogenated into saturated fatty acids, and all saturated fatty acids are decarboxylated into C ₇ ~C ₁₇ alkanes. Filter while hot to obtain long-chain alkanes and aromatics, and recover the catalyst. The method flow chart is shown in Figure 2.

For the first hydrolysis reaction, the hydrolysis rate of waste oil can be obtained by measuring the saponification value (refer to GB/T5534-2008) and acid value (refer to GB/T5530-2008) of oil. For the second step of decarboxylation and aromatization under non-hydrogen-facing conditions, fatty acids, long-chain alkanes and aromatics can be quantitatively analyzed by GC-MS-FID. The specific analysis conditions are as follows: the chromatographic column is an Agilent HP-5MS capillary column (30m×0.25mm×0.25μm), injection temperature: 300°C; injection flow rate: 11.383mL/min; injection volume: 1μL; the detection temperatures of the three detectors FID, TCD, and MS are all 300°C; Heating: keep at 50°C for 4 minutes, then raise the temperature to 190°C at a rate of 25°C/min, to 200°C at a rate of 5°C/min, to 250°C at a rate of 15°C/min, to 25°C/min The temperature was raised to 300 °C at a rate of 300 °C for 2.5 minutes.

Waste oil in the following examples was purchased from Xiamen Huayihong Import and Export Co., Ltd., quality parameters: water content<3%; iodine value: 69g I2/100g; average C-C double bond number: 0.7; saponification value: 189mg KOH/g ; Acid value: 2.9mg KOH/g; Total fat > 96%.

Example 1

Add 100g of waste oil and 50g of deionized water into a 500mL intermittent high-temperature and high-pressure reactor, start stirring, heat up to 240 ° C for 10 hours of hydrolysis reaction, after the hydrolysis reaction is completed, cool to room temperature, and obtain the upper hydrolyzate (C ₈ ~ C ₁₈ fatty acid) 86.4g; 86.4g hydrolyzate and 7.4g Pt/C were added to a 500mL intermittent high-temperature and high-pressure reactor, heated to 360°C for 5 hours, and filtered while hot to obtain 42.4g C ₇ ~C ₁₇ long Paraffins and 14.1 g aromatics.

Example 2

Add 100g of waste oil and 50g of deionized water into a 500mL intermittent high-temperature and high-pressure reactor, start stirring, heat up to 250°C for 9 hours of hydrolysis reaction, after the hydrolysis reaction is completed, cool to room temperature, and obtain the upper hydrolyzate (C ₈ ~ C ₁₈ fatty acid) 87.6g; 87.6g hydrolyzate and 8.0g Pt/C were added to a 500mL intermittent high-temperature and high-pressure reactor, heated to 360°C and reacted for 4.5h, then filtered while hot to obtain 43.2g C ₇ ~C ₁₇ Long chain alkanes and 14.7 g aromatics.

Example 3

Add 100g of waste oil and 50g of deionized water into a 500mL intermittent high-temperature and high-pressure reactor, start stirring, heat up to 260°C for 8 hours of hydrolysis reaction, after the hydrolysis reaction is completed, cool to room temperature, and obtain the upper hydrolyzate (C ₈ ~ C ₁₈ fatty acid) 88.2g; 88.2g hydrolyzate and 9g Pt/C were added to a 500mL intermittent high-temperature and high-pressure reactor, heated to 360°C for 4 hours, and filtered while hot to obtain 45.2g C ₇ ~C ₁₇ long chain Alkanes and 15.0 g aromatics.

Example 4

Add 100g of waste oil and 100g of deionized water into a 500mL intermittent high-temperature and high-pressure reactor, start stirring, heat up to 240°C for 8 hours of hydrolysis reaction, after the hydrolysis reaction is completed, cool to room temperature, and obtain the upper hydrolyzate (C ₈ ~ C ₁₈ fatty acid) 86.2g; 86.2g of hydrolyzate and 10g of Pt/C were added to a 500mL intermittent high-temperature and high-pressure reactor, heated to 360°C and reacted for 3.5h, then filtered while hot to obtain 45.3g of C ₇ ~C ₁₇ long Paraffins and 15.4 g aromatics.

Example 5

Add 100g of waste oil and 100g of deionized water into a 500mL intermittent high-temperature and high-pressure reactor, start stirring, heat up to 250°C for 7 hours of hydrolysis reaction, after the hydrolysis reaction is completed, cool to room temperature, and obtain the upper hydrolyzate (C ₈ ~ C ₁₈ fatty acid) 87.2g; 87.2g of hydrolyzate and 11g of Pt/C were added to a 500mL intermittent high-temperature and high-pressure reactor, heated to 360°C for 3 hours, and filtered while hot to obtain 45.6g of C ₇ ~C ₁₇ long chain Alkanes and 15.5 g aromatics.

Example 6

Add 100g of waste oil and 100g of deionized water into a 500mL intermittent high-temperature and high-pressure reactor, start stirring, heat up to 260°C for 6 hours of hydrolysis reaction, after the hydrolysis reaction is completed, cool to room temperature, and obtain the upper hydrolyzate (C ₈ ~ C ₁₈ fatty acid) 89.4g; 89.4g of hydrolyzate and 12g of Pt/C were added to a 500mL intermittent high-temperature and high-pressure reactor, heated to 360°C and reacted for 2.5h, then filtered while hot to obtain 47.5g of C ₇ ~C ₁₇ long Paraffins and 16.1 g aromatics.

Example 7

Add 100g of waste oil and 200g of deionized water into a 500mL intermittent high-temperature and high-pressure reactor, start stirring, heat up to 220°C for 8 hours of hydrolysis reaction, after the hydrolysis reaction is completed, cool to room temperature, and obtain the upper hydrolyzate (C ₈ ~ C ₁₈ fatty acid) 83.4g; 83.4g hydrolyzate and 13g Pt/C were added to a 500mL intermittent high-temperature and high-pressure reactor, heated to 360°C for 2 hours, and filtered while hot to obtain 45.3g C ₇ ~C ₁₇ long chain Alkanes and 15.3 g aromatics.

Example 8

Add 100g waste oil and 200g deionized water into a 500mL intermittent high-temperature and high-pressure reactor, start stirring, heat up to 240°C for 7 hours of hydrolysis reaction, after the hydrolysis reaction is completed, cool to room temperature, and obtain the upper hydrolyzate (C ₈ ~ C ₁₈ fatty acid) 93.8g; 93.8g of hydrolyzate and 14g of Pt/C were added to a 500mL intermittent high-temperature and high-pressure reactor, heated to 360°C and reacted for 1.5h, then filtered while hot to obtain 51.6g of C ₇ ~C ₁₇ long Paraffins and 17.4 g aromatics.

Example 9

Add 100g of waste oil and 200g of deionized water into a 500mL intermittent high-temperature and high-pressure reactor, start stirring, heat up to 250°C for 7 hours of hydrolysis reaction, after the hydrolysis reaction is completed, cool to room temperature, and obtain the upper hydrolyzate (C ₈ ~ C ₁₈ fatty acid) 95.6g; 95.6g hydrolyzate and 15.4g Pt/C were added to a 500mL intermittent high-temperature and high-pressure reactor, heated to 360°C for 1 hour, and filtered while hot to obtain 54.5g C ₇ ~C ₁₇ long Paraffins and 17.9 g aromatics.

Example 10

Add 100g of waste oil and 200g of deionized water into a 500mL intermittent high-temperature and high-pressure reactor, start stirring, heat up to 260°C for 6 hours of hydrolysis reaction, after the hydrolysis reaction is completed, cool to room temperature, and obtain the upper hydrolyzate (C ₈ ~ C ₁₈ fatty acid) 92.4g; 92.4g hydrolyzate and 9.2g Pt/C were added to a 500mL intermittent high-temperature and high-pressure reactor, heated to 330°C for 6 hours, and filtered while hot to obtain 47.4g C ₇ ~C ₁₇ long Paraffins and 15.7 g aromatics.

Example 11

Add 50g of waste oil and 150g of deionized water into a 500mL intermittent high-temperature and high-pressure reactor, start stirring, heat up to 220°C for 7 hours of hydrolysis reaction, after the hydrolysis reaction is completed, cool to room temperature, and obtain the upper hydrolyzate (C ₈ ~ C ₁₈ fatty acid) 46.3g; 46.3g of hydrolyzate and 3.8g of Pt/C were added to a 500mL intermittent high-temperature and high-pressure reactor, heated to 350°C for 3 hours, and filtered while hot to obtain 19.6g of C ₇ ~C ₁₇ long Paraffins and 7.5 g aromatics.

Example 12

Add 50g of waste oil and 150g of deionized water into a 500mL intermittent high-temperature and high-pressure reactor, start stirring, heat up to 250°C for 6 hours of hydrolysis reaction, after the hydrolysis reaction is completed, cool to room temperature, and obtain the upper hydrolyzate (C ₈ ~ C ₁₈ fatty acid) 46.7g; 46.7g hydrolyzate and 7.0g Pt/C were added to a 500mL intermittent high-temperature and high-pressure reactor, heated to 360°C for 4 hours, and filtered while hot to obtain 23.4g C ₇ ~C ₁₇ long Paraffins and 7.9 g aromatics.

Example 13

Add 50g of waste oil and 150g of deionized water into a 500mL intermittent high-temperature and high-pressure reactor, start stirring, heat up to 240°C for 5 hours of hydrolysis reaction, after the hydrolysis reaction is completed, cool to room temperature, and obtain the upper hydrolyzate (C ₈ ~ C ₁₈ fatty acid) 46.3g; 46.3g hydrolyzate and 8.0g Pt/C were added to a 500mL intermittent high-temperature and high-pressure reactor, heated to 270°C for 7 hours, and filtered while hot to obtain 23.6g C ₇ ~C ₁₇ long Paraffins and 8.0 g aromatics.

Example 14

Add 50g of waste oil and 150g of deionized water into a 500mL intermittent high-temperature and high-pressure reactor, start stirring, heat up to 260°C for 5 hours of hydrolysis reaction, after the hydrolysis reaction is completed, cool to room temperature, and obtain the upper hydrolyzate (C ₈ ~ C ₁₈ fatty acid) 47.2g; 47.2g of hydrolyzate and 8g of Pt/C were added to a 500mL intermittent high-temperature and high-pressure reactor, heated to 290°C for 6 hours, and filtered while hot to obtain 24.5g of C ₇ ~C ₁₇ long chain Alkanes and 8.4 g aromatics.

Example 15

Add 50g of waste oil and 200g of deionized water into a 500mL intermittent high-temperature and high-pressure reactor, start stirring, heat up to 200°C for 5 hours of hydrolysis reaction, after the hydrolysis reaction is completed, cool to room temperature, and obtain the upper hydrolyzate (C ₈ ~ C ₁₈ fatty acid) 46.7g; 46.7g hydrolyzate and 8g Pt/C were added to a 500mL intermittent high-temperature and high-pressure reactor, heated to 310°C for 5 hours, and filtered while hot to obtain 24.8g C ₇ ~C ₁₇ long chain Alkanes and 8.4 g aromatics.

Example 16

Add 50g of waste oil and 200g of deionized water into a 500mL intermittent high-temperature and high-pressure reactor, start stirring, heat up to 220°C for hydrolysis reaction for 4 hours, after the hydrolysis reaction is completed, cool to room temperature, and obtain the upper hydrolyzate (C ₈ ~ C ₁₈ fatty acid) 47.1g; 47.1g hydrolyzate and 8.0g Pt/C were added to a 500mL intermittent high-temperature and high-pressure reactor, heated to 330°C and reacted for 4 hours, then filtered while hot to obtain 29.2g C ₇ ~C ₁₇ long Paraffins and 8.9 g aromatics.

Example 17

Add 50g of waste oil and 200g of deionized water into a 500mL intermittent high-temperature and high-pressure reactor, start stirring, heat up to 240°C for 4 hours of hydrolysis reaction, after the hydrolysis reaction is completed, cool to room temperature, and obtain the upper hydrolyzate (C ₈ ~ C ₁₈ fatty acid) 48.1g; 48.1g hydrolyzate and 8.0g Pt/C were added to a 500mL intermittent high-temperature and high-pressure reactor, heated to 350°C for 3 hours, and filtered while hot to obtain 30.3g C ₇ ~C ₁₇ long Paraffins and 9.1 g aromatics.

Example 18

Add 50g of waste oil and 250g of deionized water into a 500mL intermittent high-temperature and high-pressure reactor, start stirring, heat up to 160°C for 5 hours of hydrolysis reaction, after the hydrolysis reaction is completed, cool to room temperature, and obtain the upper hydrolyzate (C ₈ ~ C ₁₈ fatty acid) 46.8g; 46.8g hydrolyzate and 8.0g Pt/C were added to a 500mL intermittent high-temperature and high-pressure reactor, heated to 370°C for 2 hours, and filtered while hot to obtain 32.4g C ₇ ~C ₁₇ long Paraffins and 9.4 g aromatics.

Example 19

Add 50g of waste oil and 250g of deionized water into a 500mL intermittent high-temperature and high-pressure reactor, start stirring, and heat up to 180°C for 4 hours of hydrolysis reaction. After the hydrolysis reaction is completed, cool to room temperature and obtain the upper hydrolyzate (C ₈ ~ C ₁₈ fatty acid) 47g; 47g hydrolyzate and 8.0g Pt/C were added to a 500mL intermittent high-temperature and high-pressure reactor, heated to 370°C for 1.0h, and then filtered while hot to obtain 31.6g C ₇ ~C ₁₇ long chain Alkanes and 9.2 g aromatics.

Claims (1)

1. a kind of method for preparing long chain alkane and aromatic hydrocarbons simultaneously by raw material of gutter oil, it is characterised in that comprise the following steps：

100g gutter oils and 200g deionized waters are added in 500mL batch (-type) high-temperature high-pressure reaction kettles, stirring is opened, is warming up to 250 DEG C of hydrolysis 7h, after hydrolysis terminates, are cooled to after room temperature, water-oil separating and obtain upper strata hydrolysate C₈~C₁₈Fat Fat acid 95.6g；

By 95.6g C₈~C₁₈Aliphatic acid and 15.4g Pt/C are added in 500mL batch (-type) high-temperature high-pressure reaction kettles, and heating rises After warm to 360 DEG C reaction 1h, 54.5g C are filtrated to get while hot₇~C₁₇Long chain alkane and 17.9g aromatic hydrocarbons.