CN111704940A - Method for preparing vehicle fuel from light coal tar - Google Patents

Method for preparing vehicle fuel from light coal tar Download PDF

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Publication number
CN111704940A
CN111704940A CN202010514603.9A CN202010514603A CN111704940A CN 111704940 A CN111704940 A CN 111704940A CN 202010514603 A CN202010514603 A CN 202010514603A CN 111704940 A CN111704940 A CN 111704940A
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fraction
light
temperature
heavy fraction
product
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陈步宁
陈锡武
程仁杰
房广信
张军
葛庆
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Xinjiang Xuanli Environmental Protection Energy Co ltd
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Xinjiang Xuanli Environmental Protection Energy Co ltd
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2270/00—Specifically adapted fuels
    • C10L2270/02—Specifically adapted fuels for internal combustion engines
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C10L2290/543—Distillation, fractionation or rectification for separating fractions, components or impurities during preparation or upgrading of a fuel

Abstract

The invention relates to a method for preparing vehicle fuel from light coal tar, which comprises the steps of fractionating the light coal tar, and adopting different isomerization treatment processes aiming at different fractionation products to obtain the vehicle fuel with high octane value, thereby realizing the full utilization of coal tar resources and having the advantages of high product purity, high yield, simple process and wide application range.

Description

Method for preparing vehicle fuel from light coal tar
Technical Field
The disclosure relates to the field of coal chemical industry, in particular to a method for preparing vehicle fuel from light coal tar.
Background
The vehicle fuel mainly comprises vehicle gasoline, vehicle diesel oil, vehicle alternative fuel (such as methanol, ethanol, emulsion fuel, natural gas, petroleum gas, hydrogen) and the like. The use performance of the vehicle fuel has direct influence on the dynamic property and the emission property of the automobile. The consumption cost of the vehicle fuel is about 1/3 of the transportation cost of the vehicle, and the economy of the vehicle is directly influenced.
The vehicle fuel mainly comprises vehicle gasoline, vehicle diesel oil, vehicle alternative fuel (such as methanol, ethanol, emulsion fuel, natural gas, petroleum gas, hydrogen) and the like. The use performance of the vehicle fuel has direct influence on the dynamic property and the emission property of the automobile. The consumption cost of the vehicle fuel is about 1/3 of the transportation cost of the vehicle, and the economy of the vehicle is directly influenced.
Octane Number (Octane Number) is an indicator of the resistance of the fuel (gasoline) used by a vehicle to knock. The gasoline contains various hydrocarbons, wherein n-heptane is easy to initiate spontaneous combustion at high temperature and high pressure, so that the phenomenon of shock explosion is caused, the efficiency of an engine is reduced, and the cylinder wall is possibly overheated and even the piston is damaged. Thus, n-heptane has an octane number of zero, and isooctane has a small knock phenomenon and an octane number of 100. Other hydrocarbons also have different octane numbers, possibly less than 0 (e.g., n-octane) and possibly greater than 100 (e.g., toluene). The octane number in gasoline is therefore directly dependent on the composition of the various hydrocarbons in the gasoline.
The characteristics of energy resources in many countries determine that coal remains the main form of energy consumption structure in many countries and the main driving force for national economic development for a long time in the future. If coal cannot be used cleanly, harmful gases such as sulfide, nitrogen oxide, carbon dioxide and the like are directly increased, and the content of suspended particles is increased. In the clean and efficient utilization route of coal, coal pyrolysis is a tap, and coal tar hydrogenation is a key. The coal tar is very similar to crude oil in composition and property, light fuel with high heat value, good thermal stability and good combustion performance can be prepared by catalytic hydrogenation under certain conditions, and vehicle fuels such as gasoline, diesel oil and the like can be obtained by a fractionation process, so that the added value and the utilization rate of products are improved, the contradiction between supply and demand of petroleum in China is relieved, and the method has important strategic significance.
However, the existing production of vehicle fuel by using coal resources has the defects of low yield and low octane number.
Disclosure of Invention
The invention provides a method for preparing vehicle fuel from light coal tar, aiming at overcoming the defects of low yield and low octane number of the conventional method for producing the vehicle fuel by utilizing coal resources.
The inventors of the present disclosure have unexpectedly found that if the light fraction, the middle fraction and the heavy fraction obtained by fractionating light coal tar under certain conditions are subjected to hydroisomerization and aromatization, respectively, the hydroisomerization efficiency of the light fraction, the middle fraction and the heavy fraction can be greatly improved, and the liquid phase products after the hydroisomerization of the three are mixed, so that a vehicle fuel with a high octane number can be obtained at a higher yield, thereby obtaining the present invention.
In order to achieve the above objects, the present disclosure provides a method for preparing a vehicle fuel from light coal tar, the method comprising: (1) carrying out first fractionation on the light coal tar to obtain a first light fraction, a first middle fraction, a first heavy fraction and a kerosene product fraction; (2) carrying out hydroisomerization on the first light fraction to obtain a first light fraction isomerization product; (3) carrying out second fractionation on the first light fraction isomerization product to obtain a second light fraction and a second heavy fraction; (4) subjecting the first middle distillate to hydroaromatization to obtain a first middle distillate aromatization product; (5) carrying out non-hydroisomerization on the first heavy fraction to obtain a first heavy fraction isomerization product; (6) performing third fractionation on the first heavy fraction isomerization product to obtain a third light fraction and a third heavy fraction; (7) subjecting the first middle distillate aromatization product to fourth fractionation to obtain a fourth light fraction and a fourth heavy fraction; (8) and mixing the second light fraction, the third heavy fraction and the fourth heavy fraction.
Optionally, in the step (1), the cut point of the first light fraction is any temperature between 80 and 95 ℃; the cutting point of the first middle distillate is any temperature between 115 and 130 ℃; the cutting point of the first heavy fraction is any temperature between 155 and 170 ℃.
Optionally, in step (2), the hydroisomerization conditions comprise: the pressure is 1.35-1.45 MPa, and the volume airspeed is 0.95-1.10 h-1The temperature is 255-270 ℃, and the hydrogen-oil ratio is 210-225: 1;
in the step (4), the hydrogen aromatization conditions comprise: the pressure is 1.8-2.5 MPa, and the volume airspeed is 1.0-1.8 h-1The temperature is 465-475 ℃, and the hydrogen-oil ratio is 950-1150: 1;
in the step (5), the non-hydroisomerization conditions comprise: the pressure is 1.4-1.8 MPa, and the volume airspeed is 1.1-1.5 h-1The temperature is 285-300 ℃, and the hydrogen-oil ratio is 850-950: 1.
Optionally, step (3) further comprises: returning the second heavy fraction to the reactor in which the hydroisomerization is carried out;
the second light fraction is an isomeride and the second heavy fraction is a non-isomeride; the second heavy fraction accounts for 10-30% of the weight of the first light fraction.
Optionally, in the step (3), the cut point of the second fractionation is any temperature between 75 and 79 ℃;
in the step (6), the cutting point of the third fractionation is any temperature between 90 and 93 ℃;
in the step (7), the cutting point of the fourth fractionation is any temperature between 200 and 220 ℃.
Optionally, the method further comprises: withdrawing the gas from the means for performing the second fractionation as a first fuel gas from the system; and leading the third light fraction out of the system as a second fuel gas.
Optionally, when the second light fraction, the third heavy fraction and the fourth heavy fraction are mixed, the weight ratio of the second light fraction, the third heavy fraction and the fourth heavy fraction is 1: 1.5-1.6: 1.3-1.4.
Optionally, the method further comprises: condensing and refluxing the fractionated fourth light fraction in a condensing tank to obtain a liquefied petroleum gas product and a hydrogen-rich gas; carrying out pressure swing adsorption separation on the hydrogen-rich gas to obtain a hydrogen product and a third fuel gas, and leading the third fuel gas out of the system;
the condensation temperature of the condensation tank is 30-40 ℃.
Optionally, the method further comprises: carrying out hydrogenation lightening treatment on coal tar to obtain a hydrogenation lightening product, and carrying out hydrogenation lightening treatment on the productSeparating the light coal tar from the light products; the conditions of the hydrogenation lightening treatment comprise: the temperature is 180-380 ℃, the pressure is 8.0-16.0 MPa, and the weight hourly space velocity is 2.0-3.0 h-1The hydrogen-oil ratio is 1200-1400: 1.
optionally, the initial boiling point of the light coal tar is any temperature between 35 and 45 ℃, and the final boiling point of the light coal tar is any temperature between 165 and 185 ℃; the density of the light coal tar is 0.72-0.775 g/mL, the carbon-hydrogen ratio is 0.3-0.4: 1.
the method fractionates the light coal tar, adopts different hydroisomerization treatment processes aiming at different fractionation products, obtains the vehicle fuel with high octane value, realizes the full utilization of coal tar resources, and has the advantages of high product purity, high yield, simple process and wide application range.
Additional features and advantages of the disclosure will be set forth in the detailed description which follows.
Drawings
The accompanying drawings, which are included to provide a further understanding of the disclosure and are incorporated in and constitute a part of this specification, illustrate embodiments of the disclosure and together with the description serve to explain the disclosure without limiting the disclosure. In the drawings:
FIG. 1 is a schematic illustration of a hydrogenation scheme according to an embodiment of the disclosure;
FIG. 2 is a schematic of a hydrogenation scheme of a comparative example of the disclosure.
Description of the reference numerals
1. Cutting tower 2, reactor one 3, reactor two
4. Reactor III 5, fractionating tower I6, fractionating tower II
7. Stabilizer column 8, reflux tank 9, pressure swing adsorption tower
10. Alkylation reactor 11, product separation tower 12, gas-liquid separation tank
13. Dehydration tower
Detailed Description
The following detailed description of specific embodiments of the present disclosure is provided in connection with the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present disclosure, are given by way of illustration and explanation only, not limitation.
As shown in fig. 1, the present disclosure provides a method for producing a vehicle fuel from light coal tar, the method comprising: (1) carrying out first fractionation on the light coal tar to obtain a first light fraction, a first middle fraction, a first heavy fraction and a kerosene product fraction; (2) carrying out hydroisomerization on the first light fraction to obtain a first light fraction isomerization product; (3) carrying out second fractionation on the first light fraction isomerization product to obtain a second light fraction and a second heavy fraction; (4) subjecting the first middle distillate to hydroaromatization to obtain a first middle distillate aromatization product; (5) carrying out non-hydroisomerization on the first heavy fraction to obtain a first heavy fraction isomerization product; (6) performing third fractionation on the first heavy fraction isomerization product to obtain a third light fraction and a third heavy fraction; (7) subjecting the first middle distillate aromatization product to fourth fractionation to obtain a fourth light fraction and a fourth heavy fraction; (8) and mixing the second light fraction, the third heavy fraction and the fourth heavy fraction.
The method fractionates the light coal tar, adopts different isomerization treatment processes aiming at different fractionation products, obtains the vehicle fuel with high octane number, realizes the full utilization of coal tar resources, and has the advantages of high product purity, high yield, simple process and wide application range.
According to the present disclosure, in order to separate different components in the light coal tar and perform different isomerization processing on the different components to prepare qualified vehicle fuel, in one embodiment, as shown in fig. 1, a cutting tower 1 may be used to cut components of a light coal tar raw material, specifically, four cutting products, i.e., a first light fraction, a first middle fraction, a first heavy fraction, and a kerosene product fraction produced at the bottom of the tower; in a further embodiment, the cut point of the first light fraction may be any temperature between 80 and 95 ℃, preferably any temperature between 82 and 93 ℃; the cutting point of the first middle distillate fraction can be any temperature between 115 and 130 ℃, and preferably can be any temperature between 120 and 125 ℃; the cutting point of the first heavy fraction can be any temperature between 155 and 170 ℃, and preferably can be any temperature between 160 and 170 ℃. The present disclosure is not limited to a specific kind of the cutting column 1 performing the first fractionation, and may be a conventional choice in the art, for example, may be a fractionation column or a rectification column.
The content of each component obtained by the first fractionation of the light coal tar is not limited, and in one embodiment, based on the total weight of the light coal tar raw material entering the fractionating tower, the content of the first light fraction may be 20 to 30 wt%, the content of the first middle fraction may be 30 to 40 wt%, the content of the first heavy fraction may be 5 to 15 wt%, and the content of the kerosene fraction may be 5 to 15 wt%; in a further embodiment, the composition of the first light fraction is C4～C6Of the first middle distillate fraction C7-C8Of the first heavy fraction, composition C of the first heavy fraction8-C9Of (4) is an organic substance.
In accordance with the present disclosure, in order to perform isomerization treatment under different conditions on different fractions obtained from the first fractionation in step (1), in one embodiment, the hydroisomerization conditions in step (2) may include: the pressure is 1.35-1.45 MPa, and the volume airspeed is 0.95-1.10 h-1The temperature is 255-270 ℃, the hydrogen-oil ratio is 210-225: 1, and preferably, the first hydroisomerization conditions can comprise: the pressure is 1.40-1.45 MPa, and the volume space velocity is 1.00-1.08 h-1The temperature is 260-265 ℃, and the hydrogen-oil ratio is 215-220: 1; in the step (4), the hydrogen aromatization conditions comprise: the pressure is 1.8-2.5 MPa, and the volume airspeed is 1.0-1.8 h-1The temperature is 465-475 ℃, and the hydrogen-oil ratio is 950-1150: 1, preferably, the second hydroisomerization conditions comprise: the pressure is 2.0-2.5 MPa, and the volume airspeed is 1.2-1.6 h-1468-472 ℃ and a hydrogen-oil ratio of 360-1100: 1; in the step (5), the non-hydroisomerization conditions comprise: the pressure is 1.4-1.8 MPa, and the volume airspeed is 1.1-1.5 h-1The temperature is 285-300 ℃, the hydrogen-oil ratio is 850-950: 1, and preferably, the third hydroisomerization conditions comprise: the pressure is 1.2-1.4 MPa, and the volume airspeed is 1.2～1.4h-1The temperature is 860-930 ℃, and the hydrogen-oil ratio is 880-920: 1.
According to the present disclosure, in order to maximize the octane number of the hydroisomerization product, as shown in fig. 1, step (3) may further comprise returning the second heavy fraction to the hydroisomerization reactor for a second hydroisomerization treatment; wherein the second light fraction is an isomeride and the second heavy fraction is a non-isomeride; in one embodiment, the second heavy fraction comprises from 10 to 30% by weight of the first light fraction, preferably the second heavy fraction comprises from 10 to 20% by weight of the first light fraction.
According to the present disclosure, in order to separate the isomerized compounds and non-isomerized compounds in the first light fraction isomerized product, in one embodiment, in step (3), the cut point of the second fractionation may be any temperature between 75 and 79 ℃, preferably, any temperature between 76 and 78 ℃; in the step (6), the cutting point of the third fractionation can be any temperature between 90 and 93 ℃, and preferably any temperature between 91 and 92 ℃; in the step (7), the cutting point of the fourth fractionation may be any temperature between 200 and 220 ℃, and preferably, any temperature between 205 and 215 ℃.
According to the present disclosure, the method further comprises: withdrawing the gas from the means for performing the second fractionation as a first fuel gas from the system; and leading the third light fraction out of the system as a second fuel gas.
The present disclosure is not limited to the types of the above catalysts used in hydroisomerization, hydroaromatization and non-hydroisomerization, and in one embodiment, the catalysts used in hydroisomerization, hydroaromatization and non-hydroisomerization may each independently be an aluminum-based modified molecular sieve supporting active component, and preferably, the molecular sieve catalyst used may contain one or more of palladium, platinum, rhenium and a rare earth element.
According to the present disclosure, in order to obtain a vehicle fuel product with a high octane number, in one embodiment, the second light fraction, the third heavy fraction, and the fourth heavy fraction may be mixed, for example, the weight ratio of the second light fraction, the third heavy fraction, and the fourth heavy fraction may be 1: 1.5 to 1.6: 1.3 to 1.4, and preferably may be 1: 1.52 to 1.57: 1.32 to 1.36.
According to the present disclosure, the method further comprises: as shown in fig. 1, condensing and refluxing the fractionated fourth light fraction in a condensing tank to obtain a liquefied petroleum gas product and a hydrogen-rich gas; carrying out pressure swing adsorption separation on the hydrogen-rich gas to obtain a hydrogen product and a third fuel gas, and leading the third fuel gas out of the system; the condensation temperature of the condensation tank is 30-40 ℃, and preferably 33-38 ℃.
The source of the light coal tar is not limited in this disclosure and may be a routine choice in the art, and in one embodiment, the source may be: carrying out hydrogenation lightening treatment on coal tar to obtain a hydrogenation lightening product, and separating the hydrogenation lightening product to obtain light coal tar; in a further embodiment, the conditions of the hydro-upgrading process may include: the temperature is 180-380 ℃, the pressure is 8.0-16.0 MPa, and the weight hourly space velocity is 2.0-3.0 h-1The hydrogen-oil ratio is 1200-1400: 1, preferably, the temperature is 220-300 ℃, the pressure is 10.0-13.0 MPa, and the weight hourly space velocity is 2.2-3.7 h-1The hydrogen-oil ratio is 1250-1350: 1.
in the embodiment of the light coal tar from coal tar hydrogenation and lightening treatment, the initial boiling point of the obtained light coal tar can be any temperature between 35 and 45 ℃, preferably any temperature between 38 and 42 ℃, and the final boiling point can be any temperature between 165 and 185 ℃, preferably any temperature between 168 and 180 ℃; the density of the light coal tar can be 0.72-0.775 g/mL, preferably 0.73-0.76 g/mL, and the carbon-hydrogen ratio can be 0.3-0.4: 1, preferably 0.33 to 0.38: 1.
the present disclosure is further illustrated by the following examples, but is not to be construed as being limited thereby.
Examples
Carrying out hydrogenation lightening treatment on coal tar, wherein the specific treatment conditions are as follows: the temperature is 220 ℃, the pressure is 11.0MPa, and the weight hourly space velocity is 2.4h-1Hydrogen-oil ratio 1300: 1; to addAnd fractionating the hydrogen product to obtain light coal tar, wherein the initial boiling point of the light coal tar is 40 ℃, the final boiling point of the light coal tar is 175 ℃, the concentration of the hydrogen is 0.73g/mL, and the carbon-hydrogen ratio of the light coal tar is 0.35: 1.
the isomerization and modification of the light coal tar are carried out by adopting the vehicle fuel preparation flow shown in figure 1:
the light coal tar is cut into four fractions by a dividing tower 1 (atmospheric fractionating tower): 25% of a first light fraction, 38% of a first intermediate fraction, 27% of a first heavy fraction and 10% of a kerosene product fraction; the cut point of the first light fraction is 85 ℃; the cut point of the first middle distillate fraction is 122 ℃; the cut point of the first heavy fraction is 163 ℃; the kerosene product fraction is not further treated and is directly taken as a product leading-out system;
carrying out hydroisomerization treatment on the first light fraction in a first reactor 2 under the following reaction conditions: the pressure is 1.42MPa, and the volume space velocity is 1.05h-1265 ℃ and a hydrogen-oil ratio of 220: 1; the yield of the first light fraction isomerized product is 98 percent, and the octane number (RON) is 88; performing second fractionation on the first light fraction isomerized product in a fractionating tower I5, wherein the cutting point of the second fractionation is 76 ℃, so as to obtain a second heavy fraction (non-isomerized product) and a second light fraction (isomerized product), returning all the second heavy fraction to a reactor I2 for secondary isomerization treatment, and simultaneously taking gas obtained in the fractionating tower I5 as a first fuel gas to be led out of the system;
and (3) carrying out hydroaromatization on the first middle distillate in a second reactor under the following reaction conditions: the pressure is 2.0MPa, and the volume space velocity is 1.5h-1The temperature is 470 ℃, and the hydrogen-oil ratio is 1100: 1; the first middle distillate isomerization product yield was 90% with an octane number (RON) of 104;
the first heavy fraction is subjected to a third hydroisomerization (hydroisomerization) in reactor three 4, under the following reaction conditions: the pressure is 1.6MPa, and the volume space velocity is 1.3h-1The temperature is 290 ℃, the hydrogen-oil ratio is 900: 1; the yield of the first heavy fraction isomerized product was 80% with an octane number (RON) of 82; subjecting the first heavy fraction isomerization product to third fractionation in a second fractionating tower 6, wherein the cutting point of the third fractionation is 92 ℃, and obtaining a third heavy fraction and a third light fraction, and taking the third light fraction as a thirdA secondary fuel gas extraction system;
subjecting the first middle distillate isomerization product to fourth fractionation in a stabilizer 7, wherein the cutting point of the fourth fractionation is 210 ℃, and obtaining a fourth heavy fraction and a fourth light fraction; mixing the second light fraction, the third heavy fraction and the fourth heavy fraction obtained in the above process to obtain the vehicle fuel, wherein the mixing weight ratio of the second light fraction, the third heavy fraction and the fourth heavy fraction is 1: 1.5: 1.1;
condensing and refluxing the fourth light fraction in a reflux tank 8 at the temperature of 36 ℃ to obtain a liquefied petroleum gas product and a hydrogen-rich gas, and leading the liquefied petroleum gas LPG as a product out of the system; introducing the hydrogen-rich gas into a pressure swing adsorption tower 9 for separation to obtain third fuel gas and hydrogen.
The yield of the vehicle fuel (octane number RON 92.17, aromatic hydrocarbon 39.6%, and benzene 0.21%) obtained in the above process was 80.43%, the yield of kerosene was 10.18%, the yield of LPG was 3.43%, the total yield of fuel gas was 3.58%, and the yield of hydrogen was 2.38%.
Comparative example
The alkylation upgrading process of the reaction of the light coal tar and the methanol as shown in figure 2 is adopted to improve the octane number of the product, and specifically:
adding light coal tar and methanol into an alkylation reactor 10 according to the weight ratio of 68:32, wherein the reaction conditions are as follows: the pressure is 0.40MPa and the temperature is 40 ℃; introducing the alkylation reaction product into a product separation tower 11, and separating to obtain a tower top light component product and a tower bottom hydrogenation product; the light component product at the top of the tower is led into a gas-liquid separation tank 12 for gas-liquid separation to obtain fuel gas and a liquid intermediate product, then the liquid intermediate product is led into a dehydration tower 13 for separation, Liquefied Petroleum Gas (LPG) is obtained at the top of the tower, and water (higher COD) is obtained at the bottom of the tower.
The yield of hydrogenation products at the bottom of the column (octane number RON 85, aromatic hydrocarbon 24.33, benzene 0.59%) was 62.2%, the total yield of fuel gas and LPG was 21.1%, and the yield of water was 16.7%.
The preferred embodiments of the present disclosure are described in detail with reference to the accompanying drawings, however, the present disclosure is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solution of the present disclosure within the technical idea of the present disclosure, and these simple modifications all belong to the protection scope of the present disclosure.
It should be noted that, in the foregoing embodiments, various features described in the above embodiments may be combined in any suitable manner, and in order to avoid unnecessary repetition, various combinations that are possible in the present disclosure are not described again.
In addition, any combination of various embodiments of the present disclosure may be made, and the same should be considered as the disclosure of the present disclosure, as long as it does not depart from the spirit of the present disclosure.

Claims (10)

1. A method for preparing vehicle fuel from light coal tar is characterized by comprising the following steps:
(1) carrying out first fractionation on the light coal tar to obtain a first light fraction, a first middle fraction, a first heavy fraction and a kerosene product fraction;
(2) carrying out hydroisomerization on the first light fraction to obtain a first light fraction isomerization product;
(3) carrying out second fractionation on the first light fraction isomerization product to obtain a second light fraction and a second heavy fraction;
(4) subjecting the first middle distillate to hydroaromatization to obtain a first middle distillate aromatization product;
(5) carrying out non-hydroisomerization on the first heavy fraction to obtain a first heavy fraction isomerization product;
(6) performing third fractionation on the first heavy fraction isomerization product to obtain a third light fraction and a third heavy fraction;
(7) subjecting the first middle distillate aromatization product to fourth fractionation to obtain a fourth light fraction and a fourth heavy fraction;
(8) and mixing the second light fraction, the third heavy fraction and the fourth heavy fraction.
2. The process according to claim 1, wherein in step (1), the cut point of the first light fraction is any temperature between 80 and 95 ℃; the cutting point of the first middle distillate is any temperature between 115 and 130 ℃; the cutting point of the first heavy fraction is any temperature between 155 and 170 ℃.
3. The method of claim 1, wherein in step (2), the hydroisomerization conditions comprise: the pressure is 1.35-1.45 MPa, the volume space velocity is 0.95-1.10 h < -1 >, the temperature is 255-270 ℃, and the hydrogen-oil ratio is 210-225: 1;
in the step (4), the hydrogen aromatization conditions comprise: the pressure is 1.8-2.5 MPa, the volume space velocity is 1.0-1.8 h < -1 >, the temperature is 465-475 ℃, and the hydrogen-oil ratio is 950-1150: 1;
in the step (5), the non-hydroisomerization conditions comprise: the pressure is 1.4-1.8 MPa, the volume space velocity is 1.1-1.5 h < -1 >, the temperature is 285-300 ℃, and the hydrogen-oil ratio is 850-950: 1.
4. The method of claim 1, wherein step (3) further comprises: returning the second heavy fraction to the reactor in which the hydroisomerization is carried out;
the second light fraction is an isomeride and the second heavy fraction is a non-isomeride; the second heavy fraction accounts for 10-30% of the weight of the first light fraction.
5. The method according to claim 1, wherein in step (3), the second fractionation has a cut point at any temperature between 75-79 ℃;
in the step (6), the cutting point of the third fractionation is any temperature between 90 and 93 ℃;
in the step (7), the cutting point of the fourth fractionation is any temperature between 200 and 220 ℃.
6. The method of claim 1, wherein the method further comprises: withdrawing the gas from the means for performing the second fractionation as a first fuel gas from the system; and leading the third light fraction out of the system as a second fuel gas.
7. The method according to claim 1, wherein when the second light fraction, the third heavy fraction and the fourth heavy fraction are mixed, the weight ratio of the second light fraction, the third heavy fraction and the fourth heavy fraction is 1: 1.5-1.6: 1.3-1.4.
8. The method of claim 1, wherein the method further comprises: condensing and refluxing the fractionated fourth light fraction in a condensing tank to obtain a liquefied petroleum gas product and a hydrogen-rich gas; carrying out pressure swing adsorption separation on the hydrogen-rich gas to obtain a hydrogen product and a third fuel gas, and leading the third fuel gas out of the system;
the condensation temperature of the condensation tank is 30-40 ℃.
9. The method of claim 1, wherein the method further comprises: carrying out hydrogenation lightening treatment on coal tar to obtain a hydrogenation lightening product, and separating the hydrogenation lightening product to obtain light coal tar; the conditions of the hydrogenation lightening treatment comprise: the temperature is 180-380 ℃, the pressure is 8.0-16.0 MPa, the weight hourly space velocity is 2.0-3.0 h < -1 >, and the hydrogen-oil ratio is 1200-1400: 1.
10. the method according to claim 9, wherein the initial boiling point of the light coal tar is any temperature between 35 and 45 ℃, and the final boiling point of the light coal tar is any temperature between 165 and 185 ℃; the density of the light coal tar is 0.72-0.775 g/mL, the carbon-hydrogen ratio is 0.3-0.4: 1.
CN202010514603.9A 2020-06-08 2020-06-08 Method for preparing vehicle fuel from light coal tar Pending CN111704940A (en)

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Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101570698A (en) * 2008-04-29 2009-11-04 中国石油化工股份有限公司 Method for catalyzing and transforming naphtha
CN110396427A (en) * 2018-04-25 2019-11-01 北京华石联合能源科技发展有限公司 A kind of processing technology of full fraction coal tar

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101570698A (en) * 2008-04-29 2009-11-04 中国石油化工股份有限公司 Method for catalyzing and transforming naphtha
CN110396427A (en) * 2018-04-25 2019-11-01 北京华石联合能源科技发展有限公司 A kind of processing technology of full fraction coal tar

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