CN114349589B - Method for preparing p-methyl ethylbenzene by using toluene and ethylene - Google Patents
Method for preparing p-methyl ethylbenzene by using toluene and ethylene Download PDFInfo
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- CN114349589B CN114349589B CN202111641309.5A CN202111641309A CN114349589B CN 114349589 B CN114349589 B CN 114349589B CN 202111641309 A CN202111641309 A CN 202111641309A CN 114349589 B CN114349589 B CN 114349589B
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- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 title claims abstract description 357
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 50
- 239000005977 Ethylene Substances 0.000 title claims abstract description 50
- JRLPEMVDPFPYPJ-UHFFFAOYSA-N 1-ethyl-4-methylbenzene Chemical compound CCC1=CC=C(C)C=C1 JRLPEMVDPFPYPJ-UHFFFAOYSA-N 0.000 title claims abstract description 23
- 238000000034 method Methods 0.000 title claims abstract description 17
- 238000006243 chemical reaction Methods 0.000 claims abstract description 72
- 239000003054 catalyst Substances 0.000 claims abstract description 14
- 238000010438 heat treatment Methods 0.000 claims abstract description 10
- 238000010791 quenching Methods 0.000 claims abstract description 10
- 230000000171 quenching effect Effects 0.000 claims abstract description 10
- 238000005804 alkylation reaction Methods 0.000 claims abstract description 9
- 238000001816 cooling Methods 0.000 claims abstract description 5
- 238000011084 recovery Methods 0.000 claims description 30
- 230000001276 controlling effect Effects 0.000 claims description 18
- 238000002156 mixing Methods 0.000 claims description 18
- HYFLWBNQFMXCPA-UHFFFAOYSA-N 1-ethyl-2-methylbenzene Chemical compound CCC1=CC=CC=C1C HYFLWBNQFMXCPA-UHFFFAOYSA-N 0.000 claims description 16
- 239000012495 reaction gas Substances 0.000 claims description 15
- 239000007789 gas Substances 0.000 claims description 9
- 125000001495 ethyl group Chemical group [H]C([H])([H])C([H])([H])* 0.000 claims description 8
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims description 6
- 239000006227 byproduct Substances 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 6
- 230000029936 alkylation Effects 0.000 claims description 5
- 239000007795 chemical reaction product Substances 0.000 claims description 5
- 239000000446 fuel Substances 0.000 claims description 4
- 239000008234 soft water Substances 0.000 claims description 3
- 238000009833 condensation Methods 0.000 claims description 2
- 230000005494 condensation Effects 0.000 claims description 2
- 238000004064 recycling Methods 0.000 claims description 2
- 230000001105 regulatory effect Effects 0.000 claims description 2
- 239000012808 vapor phase Substances 0.000 claims description 2
- 238000002360 preparation method Methods 0.000 abstract description 3
- 208000012839 conversion disease Diseases 0.000 abstract description 2
- 230000002035 prolonged effect Effects 0.000 abstract description 2
- 238000007086 side reaction Methods 0.000 abstract description 2
- 239000002994 raw material Substances 0.000 description 7
- 238000000926 separation method Methods 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- JLBJTVDPSNHSKJ-UHFFFAOYSA-N 4-Methylstyrene Chemical compound CC1=CC=C(C=C)C=C1 JLBJTVDPSNHSKJ-UHFFFAOYSA-N 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- ZLCSFXXPPANWQY-UHFFFAOYSA-N 3-ethyltoluene Chemical compound CCC1=CC=CC(C)=C1 ZLCSFXXPPANWQY-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000012295 chemical reaction liquid Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- ODLMAHJVESYWTB-UHFFFAOYSA-N ethylmethylbenzene Natural products CCCC1=CC=CC=C1 ODLMAHJVESYWTB-UHFFFAOYSA-N 0.000 description 1
- 238000004508 fractional distillation Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 238000006276 transfer reaction Methods 0.000 description 1
- 238000007039 two-step reaction Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Abstract
The invention discloses a method for preparing p-methyl ethylbenzene by using toluene and ethylene, which relates to the technical field of p-methyl ethylbenzene preparation and comprises the following steps of obtaining toluene which is in a gaseous state and is in a temperature range of 200-240 ℃, dividing the toluene into two paths, heating one path of toluene serving as main flow to 330-370 ℃ through a furnace, heating the other path of toluene serving as quenching toluene serving as a cooling source, dividing the quenching toluene into multiple sections, obtaining ethylene in addition, and dividing the ethylene into multiple sections. The alkylation reaction adopts five sections of feeding, and the temperature is raised and then lowered to make the initial temperature and the temperature rise of each section of reaction the same, so that the reaction temperature rise is avoided to be too high, the reaction can be more thoroughly carried out, the service life of the catalyst is prolonged, the reaction conversion rate is improved, and the side reaction is reduced.
Description
Technical Field
The invention relates to the technical field of preparation of p-methyl ethylbenzene, in particular to a method for preparing p-methyl ethylbenzene by using toluene and ethylene.
Background
Para-methyl ethylbenzene, also known as ethyl methyl benzene, is mainly used as a raw material for producing para-methyl styrene, which is an important unsaturated monomer, and important uses in the resin field are receiving attention.
However, as the raw material of p-methyl ethylbenzene for the production of p-methyl styrene, the existing production process is difficult to obtain high-purity p-methyl ethylbenzene raw material, or the development difficulty of the catalyst is high, or the process is complex, the energy consumption is high and the investment is high.
Disclosure of Invention
The invention mainly aims to provide a method for preparing p-methyl ethylbenzene by using toluene and ethylene, which simplifies the process steps for preparing the p-methyl ethylbenzene, ensures that the prepared p-methyl ethylbenzene has higher purity and further reduces the preparation cost.
The aim of the invention can be achieved by adopting the following technical scheme:
a method for preparing p-methyl ethylbenzene by using toluene and ethylene comprises the following steps
Step 1, obtaining toluene which is in a gaseous state and is in a temperature range of 200-240 ℃, dividing the toluene into two paths, wherein one path is taken as main flow toluene, is heated to 330-370 ℃ through a furnace, the other path is taken as quenching toluene as a cooling source, dividing the quenching toluene into a plurality of sections, and additionally obtaining ethylene and dividing the ethylene into a plurality of sections;
Step 2, mixing main stream toluene and first-stage ethylene, then entering a first reactor, controlling the temperature rise to be 20-25 ℃, and then carrying out first-stage reaction in the first reactor, wherein the reaction temperature is 350-395 ℃;
Step 3, mixing the first-stage quenched toluene and the second-stage ethylene to enter a first reactor, controlling the temperature rise to be 20-25 ℃, controlling the reaction temperature to be 330-370 ℃, and then carrying out the second-stage reaction in the first reactor;
step 4, mixing the second-stage quenched toluene and the third-stage ethylene to enter a first reactor, controlling the temperature rise to be 20-25 ℃, and then carrying out a third-stage reaction in the first reactor;
Step 5, mixing the third-stage quenched toluene and the fourth-stage ethylene to enter a first reactor, controlling the temperature rise to be 20-25 ℃, and then carrying out the fourth-stage reaction in the first reactor;
Step 6, mixing the fourth-stage quenched toluene and the fifth-stage ethylene to enter a first reactor, controlling the temperature rise to be 20-25 ℃, and then carrying out the fifth-stage reaction in the first reactor;
step 7, after the fifth reaction, the reaction gas in the first reactor enters a high-temperature heat exchanger to exchange heat with gaseous toluene, and then enters a toluene recovery tower reboiler to be used as a heat source of the toluene recovery tower;
Step 8, after the reaction products enter a toluene recovery tower, recycling toluene at the tower top to a toluene evaporator through a circulating pump to participate in the reaction again, and enabling the non-condensable gas of the reaction byproducts to enter a furnace to be combusted as fuel after passing through a toluene tower tail cooler and a water-sealed tank;
Step 9, mixing methyl ethyl benzene with tower bottom materials of the toluene recovery tower, directly feeding the mixture into an ethyl site transfer reactor for reaction, and rectifying reaction discharge to obtain the p-methyl ethyl benzene with the purity of more than 98%.
Preferably, in the step 8, a 0.32MPa steam boiler is used for condensing the gas phase of the toluene recovery tower, and the heat generated by the reaction is converted into self-generated steam and is used as a heat source of other devices.
Preferably, in the step 7, the inlet pressure of the reaction gas entering the high-temperature heat exchanger is controlled to be 0.4-0.6 MPa, and the pressure difference between the inlet pressure and the outlet pressure of the reaction gas is controlled to be less than 0.08 MPa.
Preferably, the condensate of the toluene evaporator in the step 8 is used as a soft water source for self-producing steam of the toluene recovery tower.
Preferably, in the step 9, a rectifying tower is used for rectifying, and light and heavy mixed aromatic hydrocarbon obtained in the rectifying process is collected, wherein the rectifying tower adopts the pressure of 1-10kpa and the temperature of 70-120 ℃.
Preferably, the mass ratio of the recycled toluene to the ethylene in the step 6 is 24-26, and the reaction space velocity is 0.2-0.7.
Preferably, the heating amount of the toluene recovery tower is adjusted by the amount of gaseous toluene entering the high-temperature heat exchanger in the step 7.
Preferably, in the steps 2-6, a shape selective alkylation catalyst is adopted between toluene and ethylene to catalyze and generate m-p-mixed methyl ethylbenzene.
The beneficial technical effects of the invention are as follows:
1. the invention adopts toluene circulation reaction to make the utilization rate of ethylene high, approaching 100%, and the p-methyl ethylbenzene produced by two-step reaction and separation has high quality and concentration up to above 98%.
2. In the reaction process, four steps of cooling and re-reacting are used, so that the catalyst is protected and the reaction is diluted to a certain extent, the partial pressure is reduced, and the conversion rate of the reaction is improved by utilizing the partial pressure; the reaction of the invention adopts positive pressure reaction, improves the conversion rate of the reaction, simultaneously sends tail gas as fuel to a heating furnace for combustion, and further reduces energy consumption and pollution; the rectification system (light component removal and heavy component removal tower) adopts reduced pressure rectification, so that the energy consumption and the energy quality are reduced, and the pollution to the environment is reduced.
3. The alkylation reaction adopts five sections of feeding, and the temperature is raised and then lowered to make the initial temperature and the temperature rise of each section of reaction the same, so that the reaction temperature rise is avoided to be too high, the reaction can be more thoroughly carried out, the service life of the catalyst is prolonged, the reaction conversion rate is improved, and the side reaction is reduced.
4. The invention uses the fractional distillation waste heat as the heat source of the ethyl position transfer feeding material; the process method sends the tail gas of the reaction to a heating furnace for combustion, and can save more than 30% of natural gas.
Drawings
FIG. 1 is a schematic flow diagram of a method according to an embodiment of the invention.
Detailed Description
In order to make the technical solution of the present invention more clear and obvious to those skilled in the art, the present invention will be described in further detail with reference to examples and drawings, but the embodiments of the present invention are not limited thereto.
As shown in fig. 1, the method for preparing p-methyl ethylbenzene by using toluene and ethylene provided in this example comprises the following steps,
Step 1, after raw material toluene is changed into a gas state, the raw material toluene enters a high-temperature heat exchanger to exchange heat with a reactor, the temperature is 220 ℃, then the raw material toluene is divided into two paths, one path is taken as main flow toluene and heated to 350 ℃ through a heating furnace, the other path is taken as quenching toluene and taken as a cooling source, the mass ratio of the two paths is 1:1, the quenching toluene is divided into a plurality of sections, ethylene is obtained, the ethylene is divided into a plurality of sections, and the raw material toluene is industrial toluene and industrial ethylene;
Step 2, mixing main flow toluene and first-stage ethylene, then entering a first reactor, controlling the temperature rise to 20-25 ℃, then carrying out first-stage reaction in the first reactor, wherein the reaction temperature is 375 ℃, and the toluene and ethylene react under the action of a catalyst and enter the reactor after being mixed, so that the toluene and the ethylene can be fully contacted with the catalyst at the same time, and the conversion rate and the selectivity are improved;
Step 3, mixing the first-stage quenched toluene and the second-stage ethylene, entering a first reactor, controlling the temperature rise to be 20-25 ℃, controlling the reaction temperature to be 350 ℃, and then carrying out a second-stage reaction in the first reactor;
step 4, mixing the second-stage quenched toluene and the third-stage ethylene to enter a first reactor, controlling the temperature rise to be 20-25 ℃, and then carrying out a third-stage reaction in the first reactor;
Step 5, mixing the third-stage quenched toluene and the fourth-stage ethylene to enter a first reactor, controlling the temperature rise to be 20-25 ℃, and then carrying out the fourth-stage reaction in the first reactor;
Step 6, mixing the fourth-stage quenched toluene and the fifth-stage ethylene, entering a first reactor, controlling the temperature rise to be 20-25 ℃, and then carrying out the fifth-stage reaction in the first reactor, wherein the mass ratio of the recycled toluene to the ethylene is 25, and the reaction airspeed is 0.2-0.7;
After the reaction in the step 7 and the fifth section, the reaction gas in the first reactor enters a high-temperature heat exchanger to exchange heat with gaseous toluene, wherein the gaseous toluene is the quenched toluene in the step 1, the heat exchange can reduce the load of a heating furnace, and the heat exchange can be used as a heat source of a recovery tower, if the heat exchange is not performed, the temperature of the reaction gas is too high, the reaction gas is unsuitable to enter the recovery tower, the reaction gas is a mixture after the final reaction, mainly methyl ethylbenzene and excessive toluene, and a small amount of byproducts,
Enters a toluene recovery tower reboiler, the heat of the reaction gas after heat exchange is used as a heat source of the toluene recovery tower,
The heat quantity of the toluene recovery tower is regulated by the quantity of gaseous toluene entering the high-temperature heat exchanger, the inlet pressure of the reaction gas entering the high-temperature heat exchanger is controlled to be 0.5MPa, and the pressure difference between the inlet pressure and the outlet pressure of the reaction gas is controlled to be less than 0.08 MPa;
Step 8, after the reaction product enters a toluene recovery tower, the reaction product is specifically methyl ethyl benzene, excessive toluene and trace byproducts including light aromatic hydrocarbon, heavy aromatic hydrocarbon and organic noncondensable gas, the toluene recovered from the tower top is circulated back to a toluene evaporator through a circulating pump to participate in the reaction again, and the noncondensable gas of the reaction byproduct enters a furnace to be used as fuel for combustion after passing through a toluene tower tail condenser and a water-sealed tank, wherein the noncondensable gas of the reaction byproduct mainly refers to a light organic mixture with carbon below three;
Step 9, mixing methyl ethyl benzene with tower bottom materials of a toluene recovery tower, wherein the toluene recovery tower is a separation tower, the boiling point of the mixed methyl ethyl benzene is high in the tower bottom, the mixed methyl ethyl benzene directly enters an ethyl site transfer reactor for reaction, the ethyl site transfer reactor is a second reactor, p-methyl ethyl benzene with purity of more than 98% is obtained by rectifying reaction discharge materials, and the ethyl site transfer reaction adopts mixed methyl ethyl benzene waste heat as a heat source for direct feeding;
In the embodiment, excessive toluene is separated, recycled and reacted, the separated m-p-mixed methyl-ethylbenzene enters a second reactor after heat exchange, most of m-methyl-ethylbenzene is converted into p-methyl-ethylbenzene under the action of an ethyl-site transfer catalyst, and the p-methyl-ethylbenzene with the content of more than 98% is obtained through light weight removal, heavy weight removal and rectification.
In the embodiment, in the combined steps of reaction, recovery pre-separation, re-reaction and rectification, clean recovery is adopted for the high-temperature reaction gas and the reaction process water.
In this embodiment, as shown in fig. 1, in step 2-6, toluene and ethylene are catalyzed by a shape selective alkylation catalyst to generate m-p-mixed methyl ethylbenzene;
the alkylation reaction adopts high temperature and low pressure, and excessive toluene reacts with ethylene, so that the ethylene is ensured to completely participate in the reaction, the ethylene waste is avoided, and the pressure self control is facilitated.
In the embodiment, toluene and ethylene are discharged through alkylation reaction and subjected to heat exchange, then enter a toluene reflux cylinder, enter a toluene evaporator, are heated by adopting steam of 3.8MPa, and condensate water enters a condensate tank.
In this example, the two reactors are fixed beds, and the catalyst employed is a novel alkylation catalyst and an ethyl site transfer catalyst developed by national institute.
In this example toluene and ethylene are used in the presence of a shape selective alkylation catalyst to produce m-p-mixed methyl ethylbenzene (o-methyl ethylbenzene is very slight, with an m-contrast of about 0.6).
In the embodiment, methyl ethyl benzene is mixed in a tower kettle and enters an ethyl position transfer reactor, and after reaction liquid enters a light component removal tower, light component removal is carried out;
The operation parameters of the rectifying tower A are that the pressure is 1-10Kpa, the temperature of the tower bottom is 70-120 ℃, and the temperature of the tower top is 50-70 ℃;
The kettle out enters a rectifying tower B, the rectifying tower B removes heavy components, the p-methyl ethylbenzene which is ejected to be more than 98% of the product is ejected, and the operating parameters of the rectifying tower B are as follows: the pressure is 1-10Kpa, the temperature of the tower bottom is 70-120 ℃, and the temperature of the tower top is 50-70 ℃.
In the embodiment, the vapor phase condensation of the toluene recovery tower in the step 8 adopts a 0.32MPa steam boiler to convert the heat generated by the reaction into self-produced steam, and the self-produced steam is used as a heat source of other devices.
In this example, the condensate of the toluene evaporator in step 8 was used as a soft water source for the self-produced steam of the toluene recovery column.
In this embodiment, the temperature of the toluene recovery tower can be controlled by the heat exchange amount of vaporized toluene and reaction gas, main stream toluene enters a heating furnace to be heated and vaporized ethylene to react, the reaction temperature rise is adjusted to 20-25 ℃ by the amount of ethylene, after the reaction temperature is reduced to the initial temperature of the first stage of reaction by quenching toluene, the second stage of ethylene is added to perform reaction control temperature rise, each stage of temperature rise is controlled to be the same, quenching toluene is not added after the fifth stage of reaction, the toluene enters a high temperature heat exchanger to exchange heat with vaporized toluene, and after the heat exchange reaction product enters the toluene recovery tower, toluene is ejected out of the toluene recovery tower and then is recycled to the reactor.
In the embodiment, in the step 9, a rectifying tower is used for rectifying, and the light and heavy mixed aromatic hydrocarbon obtained in the rectifying process is collected, and the light and heavy mixed aromatic hydrocarbon obtained in the rectifying process is sold or otherwise used, and the rectifying tower adopts the pressure of 1-10kpa and the temperature of 70-120 ℃.
In this example, the amount of gaseous toluene entering the high temperature heat exchanger in step 7 was used to adjust the heating capacity of the toluene recovery column.
In summary, in this embodiment, the utilization rate of ethylene by toluene circulation reaction is high, approaching 100%, and the quality of p-methyl ethylbenzene produced by two steps of reaction and separation is high, and the concentration can reach more than 98%.
The above description is merely a further embodiment of the present invention, but the protection scope of the present invention is not limited thereto, and any person skilled in the art will be able to apply equivalents and modifications according to the technical solution and the concept of the present invention within the scope of the present invention disclosed in the present invention.
Claims (1)
1. A method for preparing p-methyl ethylbenzene by using toluene and ethylene is characterized in that: comprises the following steps
Step 1, obtaining toluene which is in a gaseous state and is in a temperature range of 200-240 ℃, dividing the toluene into two paths, wherein one path is taken as main flow toluene, is heated to 330-370 ℃ through a furnace, the other path is taken as quenching toluene as a cooling source, dividing the quenching toluene into a plurality of sections, and additionally obtaining ethylene and dividing the ethylene into a plurality of sections;
Step 2, mixing main stream toluene and first-stage ethylene, then entering a first reactor, controlling the temperature rise to be 20-25 ℃, and then carrying out first-stage reaction in the first reactor, wherein the reaction temperature is 350-395 ℃;
Step 3, mixing the first-stage quenched toluene and the second-stage ethylene to enter a first reactor, controlling the temperature rise to be 20-25 ℃, controlling the reaction temperature to be 330-370 ℃, and then carrying out the second-stage reaction in the first reactor;
step 4, mixing the second-stage quenched toluene and the third-stage ethylene to enter a first reactor, controlling the temperature rise to be 20-25 ℃, and then carrying out a third-stage reaction in the first reactor;
Step 5, mixing the third-stage quenched toluene and the fourth-stage ethylene to enter a first reactor, controlling the temperature rise to be 20-25 ℃, and then carrying out the fourth-stage reaction in the first reactor;
Step 6, mixing the fourth-stage quenched toluene and the fifth-stage ethylene to enter a first reactor, controlling the temperature rise to be 20-25 ℃, and then carrying out the fifth-stage reaction in the first reactor;
step 7, after the fifth reaction, the reaction gas in the first reactor enters a high-temperature heat exchanger to exchange heat with gaseous toluene, and then enters a toluene recovery tower reboiler to be used as a heat source of the toluene recovery tower;
Step 8, after the reaction products enter a toluene recovery tower, recycling toluene at the tower top to a toluene evaporator through a circulating pump to participate in the reaction again, and enabling the non-condensable gas of the reaction byproducts to enter a furnace to be combusted as fuel after passing through a toluene tower tail cooler and a water-sealed tank;
step 9, mixing methyl ethyl benzene with tower bottom materials of a toluene recovery tower, directly entering an ethyl site transfer reactor for reaction, and rectifying reaction discharge materials to obtain p-methyl ethyl benzene with purity of more than 98%;
the vapor phase condensation of the toluene recovery tower in the step 8 adopts a 0.32MPa vapor boiler, and the heat generated by the reaction is converted into self-produced vapor and is used as a heat source of other devices;
In the step 7, the inlet pressure of the reaction gas entering the high-temperature heat exchanger is controlled to be 0.4-0.6 MPa, and the pressure difference between the inlet pressure and the outlet pressure of the reaction gas is controlled to be less than 0.08 MPa;
The condensate of the toluene evaporator in the step 8 is used as a soft water source for self-producing steam of the toluene recovery tower;
In the step 9, a rectifying tower is used for rectifying, light and heavy mixed aromatic hydrocarbon obtained in the rectifying process is collected, the pressure of the rectifying tower is 1-10kpa, and the temperature of the rectifying tower is 70-120 ℃;
the mass ratio of the circulating toluene to the ethylene in the step 6 is 24-26, and the reaction space velocity is 0.2-0.7;
The heating amount of the toluene recovery tower is regulated according to the amount of gaseous toluene entering the high-temperature heat exchanger in the step 7;
and in the steps 2-6, a shape selective alkylation catalyst is adopted between toluene and ethylene to catalyze and generate m-p-mixed methyl ethylbenzene.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111641309.5A CN114349589B (en) | 2021-12-30 | Method for preparing p-methyl ethylbenzene by using toluene and ethylene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111641309.5A CN114349589B (en) | 2021-12-30 | Method for preparing p-methyl ethylbenzene by using toluene and ethylene |
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| Publication Number | Publication Date |
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| CN114349589A CN114349589A (en) | 2022-04-15 |
| CN114349589B true CN114349589B (en) | 2024-05-14 |
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| US4732747A (en) * | 1983-04-11 | 1988-03-22 | The Dow Chemical Company | Magnesium silicate compositions and process for making |
| US4849386A (en) * | 1987-04-08 | 1989-07-18 | Taiwan Styrene Monomer Corporation | Novel silicon-modified catalyst Si/HZSM-5 preparation |
| CN102464559A (en) * | 2010-11-17 | 2012-05-23 | 中国石油化工股份有限公司 | Method for producing alkylated aromatic hydrocarbon |
| CN102464540A (en) * | 2010-11-17 | 2012-05-23 | 中国石油化工股份有限公司 | Method for producing para-alkylated arene |
| CN104230632A (en) * | 2013-06-17 | 2014-12-24 | 中国石油化工股份有限公司 | Method for producing ethyl toluene |
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| 重整C9 芳烃的综合利用;赵开鹏等;石油化工(第7期);493-493 * |
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