CN113024339A - Production process for reducing liquid carried in hydrocarbon tail gas of ethylbenzene device - Google Patents
Production process for reducing liquid carried in hydrocarbon tail gas of ethylbenzene device Download PDFInfo
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- CN113024339A CN113024339A CN202110056277.6A CN202110056277A CN113024339A CN 113024339 A CN113024339 A CN 113024339A CN 202110056277 A CN202110056277 A CN 202110056277A CN 113024339 A CN113024339 A CN 113024339A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
- C07C2/64—Addition to a carbon atom of a six-membered aromatic ring
- C07C2/66—Catalytic processes
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
- C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
- C07C5/333—Catalytic processes
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/11—Purification; Separation; Use of additives by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- C07C2523/20—Vanadium, niobium or tantalum
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- C07C2523/20—Vanadium, niobium or tantalum
- C07C2523/22—Vanadium
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- C07C2523/24—Chromium, molybdenum or tungsten
- C07C2523/28—Molybdenum
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
- C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- C07C2529/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11
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Abstract
The invention discloses a production process for reducing liquid carrying of alkylation tail gas of an ethylbenzene device, which comprises the steps of ethane separation, alkylation reaction and ethylbenzene separation, wherein the alkylation tail gas is added into a compressor and pressurized, then introduced into the bottom of an absorption tower, and sucked to the top of the absorption tower by using an absorbent, after the alkylation tail gas and the absorbent are contacted in the absorption tower, the tail gas is discharged from the top of the tower, the bottom liquid of the crude separation tower is sent to a benzene tower, non-aromatic hydrocarbons are removed, benzene is extracted, and the bottom liquid of the benzene tower is crude ethylbenzene. According to the production process for reducing the liquid carrying of the alkylation tail gas of the ethylbenzene device, the operation parameters of the rough separation tower and the absorption tower are optimized to reduce the temperature of the alkylation tail gas entering the absorption tower, so that the temperature of the top of the absorption tower is reduced, the aim of reducing the liquid carrying of the alkylation tail gas is fulfilled, the water quality of a wet air cooler is periodically analyzed every week, and the analysis result is timely adjusted to ensure the requirement of the water quality, so that the stable operation of the device can be ensured, the partial energy consumption and the material consumption of the device are reduced, and the economic benefit of a company is improved.
Description
Technical Field
The invention relates to the technical field of ethylbenzene, in particular to a production process for reducing liquid carried in alkylation tail gas of an ethylbenzene device.
Background
Ethylbenzene is an aromatic hydrocarbon, is present in coal tar and some diesel oil, is flammable, can form explosive mixtures with air, and has danger of causing combustion explosion when encountering open fire, high heat or contact with oxidant, although a small amount of ethylbenzene is present in crude oil, mass production still depends on reaction of styrene and ethylene under the catalysis of acid, the ethylbenzene is subjected to catalytic dehydrogenation to generate hydrogen and styrene, and the ethylbenzene is also present in some pigments and is mainly used for producing styrene, further producing styrene homopolymer and copolymer taking styrene as a main component, the prepared styrene is generally used for preparing common plastic products, and a small amount of styrene is used in organic synthesis industry, such as producing intermediates of acetophenone, methyl phenyl ketone and the like, is used as an intermediate of synmycin and chloramphenicol in medicine, is also used for spice, and can also be used as a solvent.
However, at present, domestic devices for preparing ethylbenzene by a dry gas method are gradually replaced by devices for preparing ethylbenzene by a liquid phase method, but for a combined device, the devices for preparing ethylbenzene by a dry gas method are necessary, and a certain amount of olefins are contained in dry gas generated by catalytic cracking of the combined device, in order to maximize the utilization of ethylene in the dry gas, only the olefins in the dry gas are consumed by the device for preparing ethylbenzene by a gas phase method, so as to produce ethylbenzene, in the process, after the amount of dry gas of an upstream device is increased, because cooling of the top of a crude separation tower is carried out by a fan, particularly in summer, the cooling effect of the fan is not good, in order to further improve the absorption effect, the amount of an absorbent has to be increased, and finally, the hydrocarbon-containing tail gas is more, so that the operation of a raw gas compressor of an aromatic hydrocarbon unit is influenced, and the furnace temperature of a heating furnace in the device is also influenced, causing fluctuations in the device.
Disclosure of Invention
The invention aims to provide a production process for reducing liquid carrying of hydrocarbon tail gas of an ethylbenzene plant, which aims to solve the problems that the prior domestic device for preparing ethylbenzene by a dry gas method is gradually replaced by a device for preparing ethylbenzene by a liquid phase method in the background art, but the device for preparing ethylbenzene by the dry gas method has the necessity for a combined device, a certain amount of olefins are contained in the dry gas generated by catalytic cracking of the combined device, in order to maximize the utilization of ethylene in the dry gas, only the olefins in the dry gas are consumed by the device for preparing ethylbenzene by the gas phase method, and then ethylbenzene is produced, in the process, after the dry gas amount of an upstream device is increased, because the cooling of the top of a crude separation tower is cooled by a fan, particularly in summer, the cooling effect of the fan is not good, in order to further improve the absorption effect, the amount of an absorbent has to be increased, and finally the hydrocarbon tail gas carries more liquid, the operation of a raw material gas compressor of an aromatic hydrocarbon unit is influenced, and the furnace temperature of a heating furnace in the device is also influenced, so that the problem of device fluctuation is caused.
In order to achieve the purpose, the invention provides the following technical scheme: a production process for reducing liquid carried in hydrocarbon tail gas of an ethylbenzene plant comprises the following steps:
the method comprises the following steps: adding the hydrocarbonized tail gas into a compressor, pressurizing, introducing into the bottom of an absorption tower, sucking the hydrocarbonized tail gas into the top of the absorption tower by using an absorbent, discharging the hydrocarbonized tail gas from the top of the absorption tower after the hydrocarbonized tail gas is contacted with the absorbent in the absorption tower, and generating a first material at the bottom of the absorption tower.
Step two: pumping the absorbent of the first material into an analytical tower for analysis, adjusting the pressure of the analytical tower, and controlling the temperature of the top of the analytical tower and the temperature of the bottom of the analytical tower.
Step three: pumping the absorbent of the resolved material I into the stabilizing tower, separating the material I from the absorbent, adjusting the pressure of the stabilizing tower, and controlling the temperature of the tower bottom and the tower top.
Step four: and mixing the gas produced at the top of the stabilizer with an oxidant and a diluent, heating, introducing the gas into a dehydrogenation reactor, and performing dehydrogenation under the action of a catalyst to obtain a material II.
Step five: and heating the material II and benzene, then feeding the heated material II and benzene into an alkylation reactor, and carrying out further reaction through catalysis to obtain a material III.
Step six: and (3) feeding the material III into a rough separation tower, removing non-aromatic hydrocarbon in a benzene tower from the bottom liquid of the rough separation tower, and extracting benzene, wherein the bottom liquid of the benzene tower is crude ethylbenzene.
Step seven: and tail gas discharged from the top of the absorption tower enters a reabsorption tower and reversely contacts with liquid diethylbenzene to absorb the absorbent in the tail gas, and after the first material is rectified in the stabilizing tower, the bottom liquid of the stabilizing tower is used as the absorbent and returns to the upper part of the absorption tower.
Step eight: the top of the coarse tower is connected with a wet air cooler, water and light hydrocarbon are removed from the tower top, the ethyl hydrocarbon on the upper part of the gas circularly enters a dehydrogenation reactor, dehydrogenation is carried out again, and the discharged tail gas enters a compressor.
Preferably, the absorbent is one or more of benzene, a stabilizer bottoms liquid, or other intermediate products of the process.
Preferably, the oxidant in the fourth step is one or a mixture of three of oxygen, fluorine and air.
Preferably, the diluent in the fourth step is one or more of clay, kaolin, pottery clay and talcum powder.
Preferably, the catalyst is Mo, V, Nb, or the active component of rare earth-containing ZSM-5 or ZSM-11 or ZSM-5/ZSM-11 co-crystallized zeolite.
Preferably, the temperature of the absorption tower and the crude separation tower is thirty-five ℃, the pressure of the crude separation tower is 0.55MpaG, and the pressure of the absorption tower is 0.5 MpaG.
Preferably, the temperature of the top of the absorption tower is twenty degrees centigrade.
Compared with the prior art, the invention has the beneficial effects that: according to the production process for reducing the liquid carrying of the alkylation tail gas of the ethylbenzene device, the operation parameters of the rough separation tower and the absorption tower are optimized to reduce the temperature of the alkylation tail gas entering the absorption tower, so that the temperature of the top of the absorption tower is reduced, the aim of reducing the liquid carrying of the alkylation tail gas is fulfilled, the water quality of a wet air cooler is periodically analyzed every week, and the analysis result is timely adjusted to ensure the requirement of the water quality, so that the stable operation of the device can be ensured, the partial energy consumption and the material consumption of the device are reduced, and the economic benefit of a company is improved.
Detailed Description
The technical solutions in the embodiments of the present invention are clearly and completely described, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The invention provides a technical scheme that: a production process for reducing liquid carried in hydrocarbon tail gas of an ethylbenzene plant comprises the following steps:
the method comprises the following steps: adding the hydrocarbonized tail gas into a compressor, performing pressurization work, pressurizing to 0.5MPaG, introducing into the bottom of an absorption tower, sucking the hydrocarbonized tail gas into the top of the absorption tower by using an absorbent, wherein the temperature of the top of the absorption tower is 20 ℃, discharging the hydrocarbonized tail gas from the top of the absorption tower after the hydrocarbonized tail gas and the absorbent are contacted in the absorption tower, and generating a material I at the bottom of the absorption tower.
Step two: pumping the absorbent of the first material into an analytical tower for analysis, adjusting the pressure of the analytical tower to be 1.25MPaG, controlling the temperature of the top of the analytical tower and the temperature of the bottom of the analytical tower, controlling the temperature of the top of the analytical tower to be 25 ℃ and the temperature of the bottom of the analytical tower to be 140 ℃.
Step three: pumping the absorbent of the resolved material I into the stabilizing tower, separating the material I from the absorbent, adjusting the pressure of the stabilizing tower, and controlling the temperature of the tower bottom and the tower top.
Step four: mixing the gas produced at the top of the stabilizer tower with an oxidant and a diluent in a molar ratio of 3: 1: 7 mixing, heating to 400 ℃, and introducing into a dehydrogenation reactor at a volume space velocity of 1800h-1And carrying out dehydrogenation work under the action of a catalyst to obtain a material II.
Step five: heating the material II and benzene to 380 ℃ at a space velocity of 1h-1And entering into an alkylation reactor for further reaction by catalysis, wherein the temperature of the alkylation reactor is 350 ℃, and the pressure is 1MPaG, so as to obtain a material III.
Step six: and (3) feeding the material III into a rough separation tower, removing non-aromatic hydrocarbon in a benzene tower from the bottom liquid of the rough separation tower, and extracting benzene, wherein the bottom liquid of the benzene tower is crude ethylbenzene.
Step seven: and tail gas discharged from the top of the absorption tower enters a reabsorption tower and reversely contacts with liquid diethylbenzene to absorb the absorbent in the tail gas, and after the first material is rectified in the stabilizing tower, the bottom liquid of the stabilizing tower is used as the absorbent and returns to the upper part of the absorption tower.
Step eight: the top of the coarse tower is connected with a wet air cooler, water and light hydrocarbon are removed from the tower top, ethylene on the upper part of the gas circularly enters a dehydrogenation reactor, dehydrogenation is carried out again, and the discharged tail gas enters a compressor.
Further, the absorbent is one or more of benzene, a stabilizing tower bottom liquid or other intermediate products of the process;
further, the oxidant in the fourth step is one or a mixture of three of oxygen, fluorine and air;
further, the diluent in the fourth step is one or more of clay, kaolin, pottery clay and talcum powder;
furthermore, the catalyst is Mo, V, Nb, or the active component of rare earth-containing ZSM-5 or ZSM-11 or ZSM-5/ZSM-11 cocrystallization zeolite;
further, the temperature of the absorption tower and the rough separation tower is thirty-five ℃, the tower pressure of the rough separation tower is 0.55MpaG, and the tower pressure of the absorption tower is 0.5 MpaG;
further, the temperature of the top of the absorption tower is twenty ℃.
The working principle is as follows: the method comprises the following steps: adding the alkylation tail gas into a compressor, performing pressurization work, pressurizing to 0.5MPaG, introducing into the bottom of an absorption tower, sucking the alkylation tail gas into the top of the absorption tower by using an absorbent, wherein the temperature of the top of the absorption tower is 20 ℃, the alkylation tail gas is discharged from the top of the absorption tower after contacting with the absorbent in the absorption tower, and a first material is generated at the bottom of the absorption tower, wherein the absorbent is one or more of benzene, a stable tower bottom liquid or other intermediate products of the process, the temperature of the absorption tower and a rough separation tower is thirty-five ℃, the pressure of the rough separation tower is 0.55MpaG, the pressure of the absorption tower is 0.5MpaG, and the second step: pumping the absorbent of the first material into an analysis tower for analysis, adjusting the pressure of the analysis tower to be 1.25MPaG, controlling the temperature of the top of the analysis tower and the temperature of the bottom of the analysis tower, controlling the temperature of the top of the analysis tower to be 25 ℃, controlling the temperature of the bottom of the analysis tower to be 140 ℃, and carrying out a third step:pumping the absorbent of the resolved material I into a stabilizing tower, separating the material I from the absorbent, adjusting the pressure of the stabilizing tower, and controlling the temperature of the tower bottom and the tower top, wherein the fourth step is that: mixing the gas produced at the top of the stabilizer tower with an oxidant and a diluent in a molar ratio of 3: 1: 7 mixing, heating to 400 ℃, and introducing into a dehydrogenation reactor at a volume space velocity of 1800h-1And carrying out dehydrogenation work under the action of a catalyst to obtain a material II, wherein an oxidant is one or a mixture of oxygen, fluorine and air, and a diluent is one or more of clay, kaolin, pottery clay and talcum powder, and the step five is as follows: heating the material II and benzene to 380 ℃ at a space velocity of 1h-1Entering into an alkylation reactor for further reaction by catalysis, wherein the temperature of the alkylation reactor is 350 ℃, and the pressure of the alkylation reactor is 1MPaG, so as to obtain a material III, wherein the catalyst is Mo, V, Nb, or an active component of rare earth-containing ZSM-5 or ZSM-11 or ZSM-5/ZSM-11 cocrystallization zeolite, and the step six is as follows: feeding the material III into a rough separation tower, removing non-aromatic hydrocarbon in a benzene tower from the bottom liquid of the rough separation tower, pumping out benzene, wherein the bottom liquid of the benzene tower is crude ethylbenzene, and the seventh step is that: and (2) enabling tail gas discharged from the top of the absorption tower to enter a reabsorption tower and reversely contact with liquid diethylbenzene to absorb the absorbent in the tail gas, rectifying the first material in a stabilizing tower, and enabling the bottom liquid of the stabilizing tower to serve as the absorbent to return to the upper part of the absorption tower, wherein the eighth step is that: the top of the coarse separation tower is connected with a wet air cooler, water and light hydrocarbon are removed from the tower top, ethylene on the upper part of the gas circularly enters a dehydrogenation reactor, dehydrogenation is carried out again, the discharged tail gas enters a compressor,
although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (7)
1. A production process for reducing liquid carried in hydrocarbon tail gas of an ethylbenzene device is characterized by comprising the following steps: the method comprises the following steps:
the method comprises the following steps: adding the alkylation tail gas into a compressor, performing pressurization work, introducing the alkylation tail gas into the bottom of an absorption tower, sucking the alkylation tail gas into the top of the absorption tower by using an absorbent, discharging the alkylation tail gas from the top of the absorption tower after the alkylation tail gas is contacted with the absorbent in the absorption tower, and generating a first material at the bottom of the absorption tower;
step two: pumping the absorbent of the first material into an analytical tower for analysis, adjusting the pressure of the analytical tower, and controlling the temperature of the top of the analytical tower and the temperature of the bottom of the analytical tower;
step three: pumping the absorbent of the resolved material I into a stabilizing tower, separating the material I from the absorbent, adjusting the pressure of the stabilizing tower, and controlling the temperature of the tower bottom and the tower top;
step four: mixing gas produced at the top of the stabilizer with an oxidant and a diluent, heating, introducing the gas into a dehydrogenation reactor, and performing dehydrogenation under the action of a catalyst to obtain a material II;
step five: heating the material II and benzene, then feeding the heated material II and benzene into an alkylation reactor, and carrying out further reaction through catalysis to obtain a material III;
step six: feeding the material III into a rough separation tower, removing non-aromatic hydrocarbon in a benzene tower from the bottom liquid of the rough separation tower, and extracting benzene, wherein the bottom liquid of the benzene tower is crude ethylbenzene;
step seven: tail gas discharged from the top of the absorption tower enters a reabsorption tower and reversely contacts with liquid diethylbenzene to absorb an absorbent in the tail gas, and after the first material is rectified in a stabilizing tower, the bottom liquid of the stabilizing tower is used as the absorbent and returns to the upper part of the absorption tower;
step eight: the top of the coarse tower is connected with a wet air cooler, water and light hydrocarbon are removed from the tower top, ethylene on the upper part of the gas circularly enters a dehydrogenation reactor, dehydrogenation is carried out again, and the discharged tail gas enters a compressor.
2. The process of claim 1, wherein the process comprises the steps of: the absorbent is one or more of benzene, a stabilizing tower bottom liquid or other intermediate products of the process.
3. The process of claim 1, wherein the process comprises the steps of: the oxidant in the fourth step is one or a mixture of oxygen, fluorine and air.
4. The process of claim 1, wherein the process comprises the steps of: and the diluent in the fourth step is one or more of clay, kaolin, argil and talcum powder.
5. The process of claim 1, wherein the process comprises the steps of: the catalyst is Mo, V, Nb, or ZSM-5 containing rare earth, or ZSM-11 or ZSM-5/ZSM-11 cocrystallization zeolite active component.
6. The process of claim 1, wherein the process comprises the steps of: the temperature of the absorption tower and the temperature of the rough separation tower are thirty-five ℃, the tower pressure of the rough separation tower is 0.55MpaG, and the tower pressure of the absorption tower is 0.5 MpaG.
7. The process of claim 1, wherein the process comprises the steps of: the temperature of the top of the absorption tower is twenty ℃.
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| CN202110056277.6A CN113024339A (en) | 2021-01-15 | 2021-01-15 | Production process for reducing liquid carried in hydrocarbon tail gas of ethylbenzene device |
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| CN202110056277.6A CN113024339A (en) | 2021-01-15 | 2021-01-15 | Production process for reducing liquid carried in hydrocarbon tail gas of ethylbenzene device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117753029A (en) * | 2023-11-27 | 2024-03-26 | 中化学科学技术研究有限公司 | Purification device and purification process |
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Application publication date: 20210625 |