CN115612525B - Process for producing light hydrocarbon and C8 aromatic hydrocarbon in high yield - Google Patents
Process for producing light hydrocarbon and C8 aromatic hydrocarbon in high yield Download PDFInfo
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- CN115612525B CN115612525B CN202110797372.1A CN202110797372A CN115612525B CN 115612525 B CN115612525 B CN 115612525B CN 202110797372 A CN202110797372 A CN 202110797372A CN 115612525 B CN115612525 B CN 115612525B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/30—Aromatics
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- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention belongs to the fields of oil refining and chemical industry, and particularly relates to a process for producing light hydrocarbon and C8 aromatic hydrocarbon in a more yield manner. The process takes C6-C11 fraction as raw material, and by arranging two sections of deep reaction units, under the action of a catalyst, the light component produced by the first section of deep reaction unit is sent to a product separation unit, and the heavy component is mixed with hydrogen-containing gas and then sent to the second section of deep reaction unit for further deep reaction. The products of the two-stage deep reaction unit are sent to a product separation unit, so that the purposes of producing more hydrogen, C2-C5 light hydrocarbons and C8 aromatic hydrocarbons are achieved. Compared with the traditional process, the process can produce more hydrogen, C2-C5 light hydrocarbon and C8 aromatic hydrocarbon, and less or no C6-C7 alkane, benzene, toluene and C9+ aromatic hydrocarbon.
Description
Technical Field
The invention belongs to the fields of oil refining and chemical industry, and particularly relates to a process for producing light hydrocarbon and C8 aromatic hydrocarbon in a more yield manner.
Background
The C6-C11 fraction is an important raw material for producing aromatic hydrocarbon and olefin products in the fields of oil refining and chemical industry, and is also an important raw material for producing high-octane gasoline components.
Under the current large environment that the crude oil processing capacity is excessive and the pressure of oil refining enterprises is reduced into gasoline, the requirement of the oil refining enterprises on transformation to the oil refining enterprises is urgent. The economic benefit of producing aromatic hydrocarbon products and olefin products by the C6-C11 fraction is better than that of producing high-octane gasoline components. Therefore, the method fully utilizes the resources of the C6-C11 fraction in the oil refining enterprises, produces more hydrogen, C2-C5 light hydrocarbon and C8 aromatic hydrocarbon, produces less or no C6-C7 alkane, benzene, toluene and C9+ aromatic hydrocarbon, is a future development trend, and is one of methods for reducing the finished gasoline and increasing the yield of olefin and aromatic hydrocarbon raw materials in the oil refining enterprises.
Disclosure of Invention
Aiming at the current situation that the yield of the aromatic hydrocarbon and olefin products is low by adopting the C6-C11 fraction as the raw material, the invention provides a process for producing more light hydrocarbon and C8 aromatic hydrocarbon, which improves the yields of products such as hydrogen, C2-C5 light hydrocarbon and C8 aromatic hydrocarbon, and the like, and produces less or no C6-C7 alkane, benzene, toluene and C9+ aromatic hydrocarbon.
In order to achieve the above object, the present invention provides a process for producing light hydrocarbons and C8 aromatic hydrocarbons in large quantities, comprising the steps of:
a) C6-C11 fraction and 1# hydrogen-containing gas are mixed and then sent to a first-stage deep reaction unit;
b) Delivering the light component produced by the first-stage deep reaction unit in the step a) to a product separation unit, mixing the heavy component with 2# hydrogen-containing gas, and delivering to a second-stage deep reaction unit;
c) And b) sending the reaction product of the two-stage deep reaction unit in the step b) to a product separation unit to obtain products comprising hydrogen-containing gas, C2-C5 light hydrocarbon, C6-C7 alkane, C8 arene, benzene, toluene, C9+ arene and C11+ heavy arene.
Preferably, the process further comprises at least one of the following treatment modes:
delivering at least one of hydrogen-containing gas, C2-C5 light hydrocarbon, C8 aromatic hydrocarbon and C11+ heavy aromatic hydrocarbon to downstream treatment;
delivering at least one of benzene, toluene, C6-C7 alkane and C9+ arene as a product, or: at least one of benzene, toluene, C6-C7 alkane and C9+ arene is sent to a first-stage deep reaction unit and/or a second-stage deep reaction unit.
In accordance with the present invention, in one embodiment, a hydrogen-containing gas is sent to a hydrogen purification unit to produce pure hydrogen and tail gas is used as a feedstock for the production of olefins.
Preferably, the hydrogen used in the first-stage deep reaction unit and the second-stage deep reaction unit are each independently selected from one of pure hydrogen and hydrogen-containing gas. The hydrogen or hydrogen-containing gas used by the first-stage deep reaction unit and the second-stage deep reaction unit can be boosted by a compressor and then sent to other processes.
Preferably, the molar ratio of the No. 1 hydrogen-containing gas to the C6-C11 fraction is 20:80-80:20.
Preferably, the reaction conditions of the one-stage deep reaction unit include: the reaction temperature is 450-550 ℃, the pressure is 0.3-1.5MPa (g), and the weight airspeed is 1-4h -1 。
As a further preferable mode, the molar ratio of the No. 1 hydrogen-containing gas to the C6-C11 fraction is 50:50-75:25.
As a further preferred embodiment, the reaction conditions of the one-stage deep reaction unit include: the reaction temperature is 500-550 ℃, the pressure is 0.3-1.0MPa (g), and the weight airspeed is 1.5-2.5h -1 。
As a preferable scheme, the molar ratio of the No. 2 hydrogen-containing gas to the heavy component is 50:50-80:20.
Preferably, the reaction conditions of the two-stage deep reaction unit include: the reaction temperature is 300-550 ℃, the pressure is 1.5-3.0MPa (g), and the weight airspeed is 1-5h -1 。
As a further preferable scheme, the molar ratio of the No. 2 hydrogen-containing gas to the heavy component is 60:40-75:25;
as a further preferred embodiment, the reaction conditions of the two-stage deep reaction unit include: the reaction temperature is 350-450 ℃, the pressure is 2.0-2.5MPa (g), and the weight space velocity is 2-3h -1 。
Preferably, the process further comprises: the reaction products of the first-stage deep reaction unit and the second-stage deep reaction unit exchange heat with the reaction feed and the C6-C11 fractions to recover heat.
Preferably, the reaction feed is heated to the reaction temperature by means of a furnace and/or a heat exchanger.
Preferably, the number of reactors used in the one-stage deep reaction unit is 1 to 8, more preferably 3 to 5; the reactors are arranged in series and/or parallel.
Preferably, the number of reactors used in the two-stage deep reaction unit is 1 to 8, more preferably 1 to 2; the reactors are arranged in series and/or parallel.
The invention has the beneficial effects that:
1. the process for producing more light hydrocarbons and C8 aromatic hydrocarbons adopts a method of deep reaction of gas and solid hydrogen, which remarkably improves the yields of products such as hydrogen, C2-C5 light hydrocarbons and C8 aromatic hydrocarbons in reaction products, and produces less or no C6-C7 alkane, benzene, toluene and C9+ aromatic hydrocarbons. The yield of ethylene and propylene can be greatly improved by sending the C2-C5 light hydrocarbon to an ethylene device as a raw material; the C8 arene is sent to the para-xylene and ortho-xylene production device, so that the yield of para-xylene and ortho-xylene can be greatly improved.
2. The process for producing light hydrocarbon and C8 aromatic hydrocarbon in a high yield can optimize the operation conditions according to market conditions and produce products such as benzene, toluene, C9+ aromatic hydrocarbon and the like. The process has flexible product proposal, short flow, small occupied area of the device and low operation cost.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The accompanying drawings are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate the invention and together with the description serve to explain, without limitation, the invention.
FIG. 1 is a schematic flow chart of the principle of the invention for producing more light hydrocarbon and C8 aromatic hydrocarbon.
Fig. 2 is a schematic flow chart of an embodiment of the present invention.
Fig. 3 is a schematic flow chart of another embodiment of the present invention.
Reference numerals illustrate:
1-C6-C11 fraction, 2-1#C6-C11 fraction, 3-heat exchanged 1#C6-C11 fraction, 4-2#C6-C11 fraction, 5-heat exchanged 2#C6-C11 fraction, 6-heat exchanged C6-C11 fraction, 7-1# hydrogen-containing gas, 8-1# hydrogen-mixed C6-C11 fraction, 9-heat exchanged 1# hydrogen-mixed C6-C11 fraction, 10-preheated 1# hydrogen-mixed C6-C11 fraction, 11-1# reaction product, 12-heat exchanged 1# reaction product, 13-1# gas phase product, 14-heat exchanged 1# gas phase product, 15-1# liquid phase product, 16-boosted 1# liquid phase product, 17-2# hydrogen-containing gas, 18-2 # hydrogen-mixed C6-C11 fraction, 19-heat-exchanged 2# hydrogen-mixed C6-C11 fraction, 20-preheated 2# hydrogen-mixed C6-C11 fraction, 21-2 # reaction product, 22-heat-exchanged 2# reaction product, 23-further heat-exchanged 2# reaction product, 24-reaction product, 25-air-cooled reaction product, 26-water-cooled reaction product, 27-2 # gas phase product, 28-hydrogen-containing gas for reaction 1, 30-boosted hydrogen-containing gas, 31-2 # liquid phase product, 32-boosted 2# liquid phase product, 33-C6-C7 alkane, 34-benzene, toluene, C9+ aromatic hydrocarbon,
101-1 heat exchanger, 102-2 heat exchanger, 103-1 heater, 104-1 reactor, 105-1 gas-liquid separator tank, 106-1 pump, 107-3 heat exchanger, 108-2 heater, 109-2 reactor, 110-4 heat exchanger, 111-air cooler, 112-water cooler, 113-2 gas-liquid separator tank, 114-1 compressor, 115-2 compressor, 116-2 pump.
Detailed Description
Preferred embodiments of the present invention will be described in more detail below. While the preferred embodiments of the present invention are described below, it should be understood that the present invention may be embodied in various forms and should not be limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the invention to those skilled in the art.
FIG. 1 is a schematic flow chart of the principle of the invention for producing more light hydrocarbon and C8 aromatic hydrocarbon. In the embodiment of the invention, the process for producing light hydrocarbon and C8 aromatic hydrocarbon in a more productive manner comprises the following steps, see FIG. 2.
a) The C6-C11 fraction 1 is divided into two streams, one stream is a C6-C11 fraction 2, and the other stream is a C6-C11 fraction 4;
b) The C6-C11 fraction 1 exchanges heat with the 1# gas phase product 13 in the 1# heat exchanger 101, and the C6-C11 fraction 2 exchanges heat with the 2# reaction product 22 after heat exchange in the 4# heat exchanger 110;
c) Mixing the heat-exchanged 1#C6-C11 fraction 3, the heat-exchanged 2#C6-C11 fraction 5 and the circulating material C6-C7 alkane 33 with the hydrogen-containing gas 7;
d) Heat exchanging the 1# hydrogen-mixed C6-C11 fraction 8 in the step C) with the 1# reaction product 11, and then sending the heat exchanged heat to a 1# heater 103 for heating;
e) Feeding the preheated 1# hydrogen-mixed C6-C11 fraction 10 in the step d) into a first-stage deep reaction unit; in the unit, the preheated 1# hydrogen-mixed C6-C11 fraction 10 is subjected to a one-stage deep reaction under the action of a catalyst;
f) The reaction product 11 of the 1# after the deep reaction in the step e) is sent to a 1# gas-liquid separation tank 105 after heat exchange with the reaction feed;
g) Exchanging heat between the 1# gas phase product 13 on the top of the 1# gas-liquid separation tank obtained in the step f) and the 1# C6-C11 fraction 2 of the raw material, and then, further cooling the mixture by an air cooler 111 and a water cooler 112, and then, delivering the mixture to a 2# gas-liquid separation tank 113;
h) Step f), the No. 1 liquid phase product 15 at the bottom of the No. 1 gas-liquid separation tank obtained in the step f) is mixed with No. 2 hydrogen-containing gas 17 after being pressurized by a No. 1 pump 106;
i) Heat exchanging the 2# hydrogen-mixed C6-C11 fraction 18 obtained in the step h) with a 2# reaction product 21, and then sending the heat exchanged heat to a 2# heater 108 for heating;
j) Feeding the preheated 2# hydrogen-mixed C6-C11 fraction 20 obtained in the step i) into a two-stage deep reaction unit; in the unit, the preheated 2# hydrogen-mixed C6-C11 fraction 20 is subjected to two-stage deep reaction under the action of a catalyst;
k) Exchanging heat between the 2# reaction product 21 obtained in the step j) and the reaction feed and then exchanging heat between the 2# reaction product 21 and the raw material 2# C6-C11 fraction 4;
l) the 2# reaction product 23 obtained in the step k) after further heat exchange is further cooled by an air cooler 111 and a water cooler 112 and then sent to a 2# gas-liquid separation tank 113;
m) taking one part of the 2# gas phase product 27 on the top of the 2# gas-liquid separation tank obtained in the step l) as the supplementary hydrogen of a first-stage deep reaction unit after being boosted by a 1# compressor 114, and taking the other part of the 2# gas phase product to be sent to a product separation unit after being boosted by a 2# compressor 115;
n) delivering a part of the hydrogen-containing gas produced by the product separation unit in the step m) to a two-stage deep reaction unit for supplementing hydrogen, and delivering the other part to a hydrogen purification unit;
o) sending the hydrogen produced by the hydrogen purification unit in the step n) to a downstream hydrogen device, and sending the tail gas to an olefin production device as a raw material;
p) the 2# liquid phase product 31 at the bottom of the 2# gas-liquid separation tank in the step l) is sent to a product separation unit after being boosted by a 2# pump 116;
q) the product separation unit in the steps m) and p), the products such as fuel gas, liquefied gas, pentane and the like are sent to a downstream olefin production device to be used as raw materials, the C8 aromatic hydrocarbon products are sent to a downstream aromatic hydrocarbon device to be used as raw materials, the C6-C7 alkane is sent to a first-stage deep reaction unit, and the products such as benzene, toluene, C9+ aromatic hydrocarbon and the like are sent to a second-stage deep reaction unit;
the composition of the catalyst, the shape and the size of the catalyst particles are not particularly limited, so long as the reaction conditions proposed by the invention are satisfied.
Example 1
As shown in fig. 2. For the raw material 1, the process for producing light hydrocarbon and C8 aromatic hydrocarbon in excess is adopted, and hydrogen, C2-C5 light hydrocarbon and C8 aromatic hydrocarbon are produced in excess through two-stage deep reaction. The operating conditions and product comparisons with conventional reactions are shown in Table 1. As can be seen from the table, the contents of hydrogen, C2-C5 light hydrocarbons, C8 aromatic hydrocarbons and other components in the reaction products are obviously higher than those in the conventional reaction, and the yields of C6-C7 alkanes, benzene, toluene and C9+ aromatic hydrocarbons are obviously reduced by the process for producing light hydrocarbons and C8 aromatic hydrocarbons in a more productive manner.
Table 1 comparison of properties
Example 2
As shown in fig. 3. For raw material 3, the comparison of the process for producing light hydrocarbons and C8 aromatic hydrocarbons with the conventional technology disclosed by the invention is shown in Table 2. As can be seen from the table, the contents of hydrogen, C2-C5 light hydrocarbon, C8 aromatic hydrocarbon and other components in the reaction product are obviously higher than those in the conventional reaction, the yields of C6-C7 alkane and C9+ aromatic hydrocarbon are obviously reduced, and partial benzene and toluene are simultaneously produced while the light hydrocarbon and the C8 aromatic hydrocarbon are produced in a more way.
Table 2 comparison of performance
The foregoing description of embodiments of the invention has been presented for purposes of illustration and description, and is not intended to be exhaustive or limited to the embodiments disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the various embodiments described.
Claims (10)
1. A process for producing light hydrocarbon and C8 aromatic hydrocarbon in a high yield is characterized by comprising the following steps:
a) C6-C11 fraction and 1# hydrogen-containing gas are mixed and then sent to a first-stage deep reaction unit;
b) Delivering the light component produced by the first-stage deep reaction unit in the step a) to a product separation unit, mixing the heavy component with 2# hydrogen-containing gas, and delivering to a second-stage deep reaction unit;
c) Sending the reaction product of the two-stage deep reaction unit in the step b) to a product separation unit to obtain a product comprising hydrogen-containing gas, C2-C5 light hydrocarbon, C6-C7 alkane, C8 arene, benzene, toluene, C9+ arene and C11+ heavy arene;
the mol ratio of the No. 1 hydrogen-containing gas to the C6-C11 fraction is 20:80-80:20;
the reaction conditions of the deep reaction unit comprise: the reaction temperature is 450-550 ℃, the pressure is 0.3-0.35MPa (g), and the weight airspeed is 1-4h -1 ；
The mol ratio of the No. 2 hydrogen-containing gas to the heavy component is 50:50-80:20;
the reaction conditions of the two-stage deep reaction unit include: the reaction temperature is 300-550 ℃, the pressure is 1.5-3.0MPa (g), and the weight airspeed is 1-5h -1 。
2. The process for the production of light hydrocarbons and C8 aromatics according to claim 1, wherein the process further comprises at least one of the following treatments:
delivering at least one of hydrogen-containing gas, C2-C5 light hydrocarbon, C8 aromatic hydrocarbon and C11+ heavy aromatic hydrocarbon to downstream treatment;
delivering at least one of benzene, toluene, C6-C7 alkane and C9+ arene as a product, or: at least one of benzene, toluene, C6-C7 alkane and C9+ arene is sent to a first-stage deep reaction unit and/or a second-stage deep reaction unit.
3. The process for the production of light hydrocarbons and C8 aromatics according to claim 1, wherein the hydrogen used in the first stage deep reaction unit and the second stage deep reaction unit are each independently selected from one of pure hydrogen and a hydrogen-containing gas.
4. The process for the production of light hydrocarbons and C8 aromatics according to claim 1, wherein,
the mol ratio of the No. 1 hydrogen-containing gas to the C6-C11 fraction is 50:50-75:25;
the reaction conditions of the deep reaction unit comprise: the reaction temperature is 500-550 ℃, and the weight space velocity is 1.5-2.5h -1 。
5. The process for the production of light hydrocarbons and C8 aromatics according to claim 1, wherein,
the mol ratio of the No. 2 hydrogen-containing gas to the heavy component is 60:40-75:25;
the reaction conditions of the two-stage deep reaction unit include: the reaction temperature is 350-450 ℃, the pressure is 2.0-2.5MPa (g), and the weight space velocity is 2-3h -1 。
6. The process for the production of light hydrocarbons and C8 aromatics according to claim 1, wherein the process further comprises:
the reaction products of the first-stage deep reaction unit and the second-stage deep reaction unit exchange heat with the reaction feed and the C6-C11 fractions to recover heat.
7. The process for the production of light hydrocarbons and C8 aromatics according to claim 1, wherein the reaction feed is heated to the reaction temperature by a furnace and/or a heat exchanger.
8. The process for the production of light hydrocarbons and C8 aromatics according to claim 1, wherein,
the number of the reactors used in the first-stage deep reaction unit is 1-8; the reactors are arranged in series and/or parallel;
the number of the reactors used by the two-stage deep reaction unit is 1-8; the reactors are arranged in series and/or parallel.
9. The process for the production of light hydrocarbons and C8 aromatics according to claim 8, wherein the number of reactors used in the first stage of the deep reaction unit is 3 to 5.
10. The process for the production of light hydrocarbons and C8 aromatics according to claim 8, wherein the number of reactors used in the two-stage deep reaction unit is 1-2.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101734986A (en) * | 2008-11-21 | 2010-06-16 | 中国石油化工股份有限公司 | Method for hydrogenation pyrolysis of prolific benzene and xylene by using pyrolysis gasoline |
| CN103880584A (en) * | 2012-12-19 | 2014-06-25 | 中国石油化工股份有限公司 | Method for combined production of p-xylene |
| CN106588558A (en) * | 2015-10-19 | 2017-04-26 | 中国石油化工股份有限公司 | Method for increasing production of xylene through arene alkyl transfer and light aromatics |
| CN112771137A (en) * | 2018-10-25 | 2021-05-07 | 沙特阿拉伯石油公司 | Process and system for producing para-xylene and benzene from a stream rich in C6 to C12+ aromatic hydrocarbons |
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- 2021-07-14 CN CN202110797372.1A patent/CN115612525B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101734986A (en) * | 2008-11-21 | 2010-06-16 | 中国石油化工股份有限公司 | Method for hydrogenation pyrolysis of prolific benzene and xylene by using pyrolysis gasoline |
| CN103880584A (en) * | 2012-12-19 | 2014-06-25 | 中国石油化工股份有限公司 | Method for combined production of p-xylene |
| CN106588558A (en) * | 2015-10-19 | 2017-04-26 | 中国石油化工股份有限公司 | Method for increasing production of xylene through arene alkyl transfer and light aromatics |
| CN112771137A (en) * | 2018-10-25 | 2021-05-07 | 沙特阿拉伯石油公司 | Process and system for producing para-xylene and benzene from a stream rich in C6 to C12+ aromatic hydrocarbons |
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