CN112194553B - Method and device for separating mixture of carbon nine aromatic hydrocarbon - Google Patents
Method and device for separating mixture of carbon nine aromatic hydrocarbon Download PDFInfo
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- CN112194553B CN112194553B CN202011218310.2A CN202011218310A CN112194553B CN 112194553 B CN112194553 B CN 112194553B CN 202011218310 A CN202011218310 A CN 202011218310A CN 112194553 B CN112194553 B CN 112194553B
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- C07C7/04—Purification; Separation; Use of additives by distillation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
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- C07C7/005—Processes comprising at least two steps in series
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
- C07C7/05—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds
- C07C7/08—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds by extractive distillation
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Abstract
The invention belongs to the technical field of separation of polymethyl aromatic compounds, and particularly relates to a method and a device for separating a mixture of carbon nine aromatic compounds. The method comprises the following steps: introducing light components containing the mesitylene and at least one of the p-methyl cumene and the indane into a mesitylene extraction rectifying tower, carrying out extractive rectification in the presence of a second extractant, extracting the at least one of the p-methyl cumene and the indane from the top of the mesitylene extraction rectifying tower, and extracting heavy components containing the second extractant and the mesitylene from the bottom of the tower; the second extractant is a mixed solution of 3,4, 5-trimethylphenol and n-octanol. The method and the device provided by the invention can separate and purify the effective components in the byproduct resources of the refinery, the application range of the product is wide, the added value is greatly improved, and the comprehensive utilization of the precious resources is realized.
Description
Technical Field
The invention belongs to the technical field of separation of polymethyl aromatic compounds, and particularly relates to a method and a device for separating a mixture of carbon nine aromatic compounds.
Background
Large refinery aromatics complex has a large number of reformed carbon nine-fold aromatics resources that are complex in composition, typically having more than forty components, with different components having different uses. The economic value of the components is generally not more than three, the existing technology only extracts one component of the trimellitic benzene, the rest components are used as raw materials of aromatic hydrocarbon solvents or other purposes, and more components with higher economic value are not well separated and purified due to the limitations of technology and equipment, so that the resources are greatly wasted.
Disclosure of Invention
Aiming at the defects of the prior art, the invention aims to provide a method and a device for separating a carbon nine aromatic hydrocarbon mixture, which can separate components of pseudocumene, mesitylene, hemimellitene and o-methyl ethylbenzene in the carbon nine aromatic hydrocarbon mixture system, realize the separation, purification and comprehensive utilization of high added value components in byproduct carbon nine heavy aromatic hydrocarbon of a large refinery aromatic hydrocarbon combined device, and are energy-saving, emission-reducing and environment-friendly.
Specifically, the invention provides the following technical scheme.
A process for separating a mixture of carbon nonaarenes containing pseudocumene, mesitylene and at least one member selected from the group consisting of p-methyl cumene and indane, said process comprising the steps of:
(1) Introducing heavy components with the boiling point higher than 165.5 ℃ in the carbon nona-arene mixture into a pseudocumene rectifying tower, leading out pseudocumene products from the side line of the pseudocumene rectifying tower, leading out light components with the boiling point between 165.5 and 169.3 ℃ from the top of the tower, and leading out heavy components with the boiling point higher than 170 ℃ from the bottom of the tower;
(2) Introducing the heavy component with the boiling point higher than 170 ℃ in the step (1) into a hemimellitene light component removing tower, extracting light component with the boiling point between 170 and 176 ℃ from the top of the hemimellitene light component removing tower, and extracting the heavy component with the boiling point higher than 176 ℃ from the bottom of the tower;
(3) Introducing the heavy component with the boiling point higher than 176 ℃ in the step (2) into a de-trimethyl benzene tower, extracting light components containing the de-trimethyl benzene and at least one of p-methyl cumene and indane from the top of the de-trimethyl benzene tower, and extracting the heavy component with the boiling point higher than 177.2 ℃ from the bottom of the tower;
(4) Introducing the light component in the step (3) into a hemimellitene extractive distillation column, carrying out extractive distillation in the presence of a second extractant, extracting at least one selected from p-methyl isopropylbenzene and indane from the top of the hemimellitene extractive distillation column, and extracting a heavy component containing the second extractant and the hemimellitene from the bottom of the column;
wherein the second extractant is a mixed solution comprising 3,4, 5-trimethylphenol and n-octanol.
According to the invention, by utilizing the different properties of component molecular structures, a proper polar solvent of a binary system of 3,4, 5-trimethylphenol and n-octanol is selected as an extractant, and mesitylene with very similar boiling points and difficult separation by superfraction is skillfully separated from indane and p-methyl cumene.
Preferably, in the above method for separating a mixture of carbon nonaarenes, the molar ratio of 3,4, 5-trimethylphenol to n-octanol is 1.5-2.5:1, more preferably 1.8-2.2:1.
Preferably, the above method for separating a mixture of carbon nonaarenes further comprises the following steps: introducing the heavy component containing the second extractant and the hemimellitene in the step (4) into a hemimellitene resolving tower, leading out the hemimellitene product from the top of the hemimellitene resolving tower, and leading out the second extractant from the bottom of the tower.
Preferably, in the above method for separating a mixture of carbon nonaarenes, the mixture of carbon nonaarenes further contains mesitylene and o-methyl ethylbenzene, and the method further comprises the following steps:
(5) Introducing the mixture of the carbon nine aromatic hydrocarbon into a first light component removing tower, extracting light components with boiling point lower than 164.5 ℃ from the top of the first light component removing tower, and extracting heavy components containing mesitylene and o-methyl ethylbenzene from the bottom of the tower;
(6) Introducing the heavy component in the step (5) into a mesitylene removing tower, extracting light components containing mesitylene and o-methyl ethylbenzene from the top of the mesitylene removing tower, and extracting the heavy component with the boiling point higher than 165.5 ℃ from the bottom of the tower;
(7) Introducing the light component containing the mesitylene and the o-methyl ethylbenzene in the step (6) into a mesitylene extraction and rectification tower, carrying out extraction and rectification in the presence of a first extractant, leading out an o-methyl ethylbenzene product from the top of the mesitylene extraction and rectification tower, and leading out heavy component containing the first extractant and the mesitylene from the bottom of the tower;
wherein the first extractant is a mixed solution comprising trimesic acid trimethyl and n-octanol, more preferably, the molar ratio of trimesic acid trimethyl to n-octanol is 3-5:1, even more preferably 3.5-4.5:1, and most preferably 3.8-4.2:1.
Preferably, the above method for separating a mixture of carbon nonaarenes further comprises the following steps: introducing the heavy component containing the first extractant and the mesitylene in the step (7) into a mesitylene analysis tower, leading out a mesitylene product from the top of the mesitylene analysis tower, and leading out the first extractant from the tower bottom.
The invention also provides a device for separating the mixture of the carbon nine aromatic hydrocarbon, which comprises a pseudocumene rectifying tower, a pseudocumene light component removing tower, a pseudocumene extracting rectifying tower and a pseudocumene analyzing tower;
The side part of the pseudocumene rectifying tower is provided with a raw material feed inlet, and the raw material feed inlet of the pseudocumene rectifying tower is used for inputting heavy components with boiling points higher than 165.5 ℃ in the carbon nonaromatic hydrocarbon mixture;
the off-trimethylbenzene rectifying tower is provided with a side line discharge port, off-trimethylbenzene products are led out from the side line discharge port, and a tower bottom discharge port of the off-trimethylbenzene rectifying tower is connected with a raw material feed port of the continuous trimethylbenzene light component removing tower;
the tower bottom discharge port of the hemimellitene light component removing tower is connected with the raw material feed port of the hemimellitene component removing tower;
the top discharge port of the hemimellitene removing tower is connected with the raw material feed port of the hemimellitene extracting and rectifying tower;
the second extractant feed inlet is arranged in the hemimellitene extraction rectifying tower, the methyl cumene and/or indane is led out from the top discharge port of the hemimellitene extraction rectifying tower, and the bottom discharge port of the tower is connected with the raw material feed inlet of the hemimellitene analyzing tower;
and a hemimellitene product is led out from a top discharge port of the hemimellitene resolving tower.
Preferably, in the device for separating the mixture of the carbon and the nonaromatic hydrocarbon, at least a packing or a column plate with the height equivalent to eight theoretical column plates is arranged between a side line discharge port of the trimellitic rectifying column and the top of the side line discharge port.
Preferably, the device for separating the mixture of carbon and nine aromatic hydrocarbon further comprises a first light component removing tower, a mesitylene extracting and rectifying tower and a mesitylene analyzing tower;
the side part of the first light component removing tower is provided with a carbon nine-aromatic hydrocarbon mixture feed inlet, and a tower bottom discharge port of the first light component removing tower is connected with a raw material feed inlet of the mesitylene removing tower;
the top discharge port of the mesitylene removing tower is connected with the raw material feed port of the mesitylene extracting and rectifying tower; the tower kettle discharge port of the mesitylene removing tower is connected with the raw material feed port of the pseudocumene rectifying tower;
the mesitylene extraction rectifying tower is provided with a first extractant feed inlet, an o-methyl ethylbenzene product is led out from the top discharge port of the mesitylene extraction rectifying tower, and the bottom discharge port of the mesitylene extraction rectifying tower is connected with the raw material feed inlet of the mesitylene analysis tower;
and a mesitylene product is led out from a top discharge port of the mesitylene analysis tower.
Preferably, in the device for separating a mixture of carbon and nine aromatic hydrocarbons, the first light component removing tower, the mesitylene component extracting and rectifying tower, the hemimellitene component removing tower and the hemimellitene component extracting and rectifying tower are filled with bidirectional curvedly wave efficient structured packing;
And the inner parts of the mesitylene analysis tower, the pseudocumene rectification tower and the hemimellitene analysis tower are filled with bidirectional oblique wave efficient structured packing.
The invention also provides a method for separating mesitylene from at least one selected from p-methyl cumene and indane, which comprises the following steps: extracting and rectifying a system containing mesitylene and at least one of p-methyl isopropylbenzene and indane in the presence of an extracting agent, wherein the extracting agent is a mixed solution comprising 3,4, 5-trimethylphenol and n-octanol; more preferably, the molar ratio of 3,4, 5-trimethylphenol to n-octanol is 1.5-2.5:1, still more preferably 1.8-2.2:1.
The beneficial effects obtained by the invention are as follows:
the method and the device provided by the invention can separate and purify the effective components in the byproduct resources of the refinery, the application range of the product is wide, the added value is greatly improved, and the comprehensive utilization of the precious resources is realized.
Drawings
FIG. 1 is a schematic view of an apparatus according to an embodiment; wherein, 1, a raw material conveying pump, 2, a first light component removing tower, 3, a light component conveying pump, 4, a first light component removing tower kettle conveying pump, 5, a mesitylene removing tower, 6, an enriched mesitylene conveying pump, 7, a mesitylene removing tower kettle component conveying pump, 8, a pseudocumene rectifying tower, 9, a pseudocumene product conveying pump, 10, a pseudocumene rectifying tower kettle component conveying pump, 11, a first extractant conveying pump, 12, a mesitylene extracting and rectifying tower, 13, an enriched o-methyl ethylbenzene conveying pump, 14, a mesitylene extracting and rectifying tower kettle component conveying pump, 15, a mesitylene analyzing tower, 16, a mesitylene product conveying pump, 17, a mesitylene analyzing tower kettle first extractant conveying pump, 18, a component conveying pump with the boiling point of 165.5-169.3 ℃,19, a hemimellitene light component removing tower, 20, a component conveying pump with the boiling point of 170-176 ℃,21, a hemimellitene light component conveying pump, 22, a hemimellitene removing tower, 23, an enriched hemimellitene conveying pump, 24, a hemimellitene removing tower kettle component conveying pump, 25, a second extractant conveying pump, 26, a hemimellitene extraction rectifying tower, 27, an indane and methyl isopropylbenzene conveying pump, 28, a hemimellitene extraction rectifying tower kettle component conveying pump, 29, a hemimellitene resolving tower, 30, a hemimellitene product conveying pump, 31 and a hemimellitene resolving tower kettle second extractant conveying pump.
FIG. 2 is a gas chromatogram of the end product of example 1, pseudocumene.
FIG. 3 is a gas chromatogram of mesitylene as the final product in example 1.
FIG. 4 is a gas chromatogram of the final product of mesitylene in example 1.
FIG. 5 is a gas chromatogram of the final product, o-methyl ethylbenzene in example 1.
Detailed Description
Aiming at the defect that high added value components in the carbon nine-heavy aromatic hydrocarbon cannot be effectively separated and purified in the prior art, the invention provides a method and a device for separating a carbon nine-aromatic hydrocarbon mixture, which realize the separation and purification and comprehensive utilization of the components of the meta-trimethyl benzene, the mesitylene, the hemimellitene and the o-methyl ethylbenzene in the byproduct carbon nine-heavy aromatic hydrocarbon in a large refinery aromatic hydrocarbon combined device, and are energy-saving, emission-reducing and environment-friendly.
According to the method, a refinery reformed carbon nine-heavy aromatic hydrocarbon raw material is firstly added into a rectifying tower provided with internal components at a certain speed, and light components with lower boiling points than mesitylene are removed under specific temperature, pressure and reflux conditions.
The carbon nine-heavy aromatic hydrocarbon with light components removed is fed into a rectifying tower with internal components at a certain speed, and under the specific conditions of temperature, pressure and reflux, mesitylene and o-methyl ethylbenzene with the boiling point very close to that of mesitylene are distilled out from the top of the tower and fed into an extraction rectifying tower. In the extractive distillation column, the binary extractant system absorbs mesitylene but not o-methyl ethylbenzene. O-methyl-ethylbenzene-rich vapor is distilled off from the top of the column as a byproduct. The rich liquid of the extractant absorbing the mesitylene is sent into an analysis tower according to a certain speed, and under specific temperature, pressure and reflux conditions, the high-purity mesitylene is analyzed as a product and escapes from the tower top. The lean extract liquid in the tower bottom returns to the extraction rectifying tower again for recycling.
The carbon nine-heavy aromatic hydrocarbon from which the mesitylene and the o-methyl ethylbenzene which is very close to the boiling point thereof are removed enters a rectifying tower with internal components at a certain speed, and under specific temperature, pressure and reflux conditions, high-purity meta-trimethylbenzene products are extracted from a side line near the top of the tower, and the gas phase at the top of the tower is a component with the boiling point between that of the meta-trimethylbenzene and the mesitylene (containing o-toluene). The tower bottom is a component with boiling point higher than that of the pseudocumene.
The residual carbon nine-heavy aromatic hydrocarbon after removing the components of the pseudocumene enters a rectifying tower with internal components at a certain speed, and the components with boiling points between the pseudocumene and the hemimellitene are removed at the top of the tower under specific temperature, pressure and reflux conditions. The column bottoms are components containing mesitylene and having a boiling point higher than that of mesitylene. Feeding into a rectifying tower with internal components at a certain speed, and under specific temperature, pressure and reflux conditions, the components distilled from the tower top are mesitylene, indane and p-methyl isopropylbenzene with the boiling point close to that of mesitylene. Feeding the mixture into an extraction rectifying tower with internal components at a certain speed. The column bottoms yield other components boiling more than mesitylene (containing indane and p-methyl cumene).
In the extractive distillation column, the binary extractant system absorbs hemimellitene but not indane and p-methyl cumene at specific temperature, pressure and reflux conditions. The indane-rich and p-methyl cumene vapors are distilled off from the top of the column as by-products. The rich liquid of the extractant absorbing the hemimellitene is sent into a resolving tower at a certain speed, and the high-purity hemimellitene is resolved out under specific temperature, pressure and reflux conditions and escapes from the tower top. The lean liquid in the tower bottom returns to the extraction rectifying tower again for recycling.
Through the steps, the complete separation of three trimethylbenzenes in the reformed carbon nine raw materials is completed, and the maximum effective utilization of resources is realized. The key is that the invention uses the property of very close boiling point and different molecular structures of components difficult to separate by superfractionation to select proper binary system polar solvent as extractant, and skillfully separates mesitylene from o-methyl ethylbenzene; and (3) separating the hemimellitene from the indane and the p-methyl isopropylbenzene.
Meanwhile, the technical scheme provided by the invention is more suitable for industrial production, and a super rectification technology, an extraction rectification technology, a thermal coupling technology and a thermal integration technology are used. Specifically, the trimellitic column is designed to be positive pressure, and the trimellitic steam at the side line of the column can be led back to a reboiler of the light component removal column to be used as a heat source to form thermal coupling; introducing o-methyl ethylbenzene steam at the top of the mesitylene extraction rectifying tower back to a heat source of a three-tower reboiler for removing the mesitylene to form thermal coupling; the indane and the p-methyl isopropylbenzene steam at the top of the hemimellitene extraction rectifying tower are led back to a heat source of a three-tower reboiler for removing the coupling to form thermal coupling; the steam condensate is collected according to the temperature steps and then used as a multi-section raw material, a semi-finished product feeding preheating heat source and a heat tracing heat source, so that the energy steps are utilized effectively. The energy consumption is saved, so that the production cost is effectively reduced, the whole production process is easy to control, the continuous operation is stable, the separation precision is high, the product purity is high, the product quality is reliable, the target product yield is high, and the method can be widely applied to the full separation of high-added-value pseudocumene, mesitylene and hemimellitene from the byproduct reformed carbon nine-heavy aromatics of a large-scale oil refinery so as to realize the efficient comprehensive utilization of precious resources.
In a preferred embodiment, as shown in fig. 1, the device for separating a carbon nonaarene mixture provided by the invention comprises a raw material conveying pump 1, a first light component conveying pump 2, a light component conveying pump 3, a first light component conveying pump 4, a mesitylene removing tower 5, an enriched mesitylene conveying pump 6, a mesitylene removing tower kettle component conveying pump 7, a mesitylene rectifying tower 8, a mesitylene product conveying pump 9, a mesitylene rectifying tower kettle component conveying pump 10, a first extractant conveying pump 11, a mesitylene extracting rectifying tower 12, an enriched o-ethylbenzene conveying pump 13, a mesitylene extracting rectifying tower kettle component conveying pump 14, a mesitylene resolving tower 15, a mesitylene product conveying pump 16, a mesitylene resolving tower kettle first extractant conveying pump 17, a boiling point 165.5-169.3 ℃ component conveying pump 18, a mesitylene removing tower 19, a component conveying pump 20 with a temperature of 170-176 ℃, a mesitylene light component conveying pump 21, a mesitylene removing tower component conveying pump 22, an enriched mesitylene stripping tower 22, a mesitylene stripping tower 25, a mesitylene separating tower second pump 25, a mesitylene separating tower 25, a mesitylene separating pump 25 and a mesitylene separating tower component conveying pump 25.
The side part of the first light component removing tower 2 is provided with a carbon nine-aromatic hydrocarbon mixture feed inlet, and a tower bottom discharge outlet of the first light component removing tower 2 is connected with a raw material feed inlet of the mesitylene removing tower 5;
the top discharge port of the mesitylene removing tower 5 is connected with the raw material feed port of the mesitylene extracting and rectifying tower 12;
the mesitylene extraction rectifying tower 12 is provided with a first extractant feed inlet, an o-methyl ethylbenzene product is led out from a top discharge port of the mesitylene extraction rectifying tower 12, and a tower bottom discharge port is connected with a raw material feed inlet of the mesitylene analyzing tower 15;
the discharge port of the tower kettle of the mesitylene removing tower 5 is connected with the raw material feed port of the pseudocumene rectifying tower 8;
the pseudocumene rectifying tower 8 is provided with a side-line discharge port, a pseudocumene product is led out from the side-line discharge port, and a tower bottom discharge port of the pseudocumene rectifying tower 8 is connected with a raw material feed port of the hemimellitic light component removing tower 19;
the tower bottom discharge port of the hemimellitene light component removing tower 19 is connected with the raw material feed port of the hemimellitene removing tower 22;
the top discharge port of the hemimellitene removing tower 22 is connected with the raw material feed port of the hemimellitene extracting and rectifying tower 26;
the hemimellitene extraction rectifying tower 26 is provided with a second extractant feed inlet, the top discharge port of the hemimellitene extraction rectifying tower 26 is led out of the methyl cumene and the indane, and the bottom discharge port is connected with the raw material feed inlet of the hemimellitene analyzing tower 29;
And a hemimellitene product is led out from the top discharge port of the hemimellitene resolving tower 29.
In a preferred embodiment, the parameters of the first light ends column 2 include: the inner diameter is 3.8 meters, the height of CHAAPAKAK 6.0 high-efficiency structured packing is 40 meters (divided into nine sections, matched distributor, supporting ring and other internal parts), the number of theoretical plates is 100, and the tangential height of a tower body is 58.5 meters;
the parameters of the mesitylene-free tower 5 include: the inner diameter is 2.6 meters, the height of CHAAPAKAK 6.0 high-efficiency structured packing is 44 meters (divided into eight sections, matched distributor, supporting ring and other internal parts), the number of theoretical plates is 86, and the tangential height of a tower body is 62 meters;
the parameters of the pseudocumene rectifying column 8 include: the inner diameter is 2.2 meters, the height of ZUPAK5.0 high-efficiency structured packing is 34 meters (divided into nine sections, matched distributor, supporting ring and other internal parts), the number of theoretical plates is 76, and the tangential height of a tower body is 44.6 meters; the lateral line discharge port of the pseudocumene rectifying tower 8 is arranged on a liquid collecting disc at the lower part of the second section of packing;
the mesitylene extraction rectifying tower 12 parameters include: the inner diameter is 1.6 meters, the height of CHAAPAKAK 5.0 high-efficiency structured packing is 22 meters (divided into five sections, matched distributor, supporting ring and other internal parts), the number of theoretical plates is 40, and the tangential height of a tower body is 28 meters;
the inner diameter of the mesitylene analysis tower 15 is 1.2 m, the height of ZUPAK5.0 efficient structured packing is 18.6 m (divided into four sections, matched internal parts such as a distributor, a supporting ring and the like), the number of theoretical plates is 32, and the tangent height of a tower body is 24.4 m;
The inner diameter of the hemimellitene light component removal tower 19 is 2 meters, the height of CHAAPAK 6.0 high-efficiency structured packing is 28.5 meters (divided into five sections, matched internal components such as a distributor, a supporting ring and the like), the number of theoretical plates is 60, and the tangent height of a tower body is 33.6 meters;
the inner diameter of the deironing trimethyl benzene tower 22 is 1.0 m, the height of CHAAPAK 6.0 efficient structured packing is 26.6 m (divided into eight sections, matched internal parts such as a distributor, a supporting ring and the like), the number of theoretical plates is 50, and the tangent height of a tower body is 33.6 m;
parameters of the hemimellitene extractive distillation column 26 include: the inner diameter is 1.4 meters, the height of CHAAPAKAK 5.0 high-efficiency structured packing is 23.6 meters (divided into five sections, matched internal parts such as a distributor, a supporting ring and the like), the number of theoretical plates is 42, and the tangential height of a tower body is 30 meters;
the inner diameter of the mesitylene analysis tower 29 is 1.0 m, the height of ZUPAK5.0 efficient structured packing is 16.8 m (divided into four sections, matched internal parts such as a distributor, a supporting ring and the like), the number of theoretical plates is 30, and the tangent height of the tower body is 22.6 m.
The CHAAPAKAK and ZUPAK high-efficiency structured packing is obtained from Tianjin Datian Jiujingsu Co.
The various columns described above, with attached reboiler/condenser/reflux drum/reflux pump-metering and transporting systems, are the equipment required for standard (super) rectification units. The conveying units all select chemical process pumps.
The method for separating the mixture of the carbon nonaromatic hydrocarbons by adopting the device comprises the following steps:
(1) The byproduct reformed carbon nine-heavy aromatic hydrocarbon of the oil refinery is fed into a first light component removing tower 2 at the speed of 80-120 kmol/h, and under the operating conditions of the tower top pressure of 10-20 kPa. A, the temperature of 95-115 ℃ and the reflux ratio of 3-4:1, the components with the boiling point lower than 164.5 ℃ (namely the components lower than mesitylene) are removed from the tower top, and can be used as SA1000# aromatic hydrocarbon solvent products, and the content of the mesitylene carried by the tower top components is lower than 2% (wt). The tower bottom is composed of mesitylene and components with boiling point higher than that of the mesitylene, the content of light components is lower than 0.5%, the heating source for the initial operation of the first light component removing tower 2 is external steam, and after the pseudocumene rectifying tower 8 is normal, the pseudocumene steam is introduced as the heating source;
(2) And (3) feeding the tower kettle component obtained by the first light component removing tower 2 into the mesitylene removing tower 5 at the speed of 60-90 kmol/h. And removing mesitylene and o-methyl ethylbenzene components with the boiling point close to the mesitylene from the tower top under the operation conditions of the tower top pressure of 5-10 kPa.A, the temperature of 105-118 ℃ and the reflux ratio of 4-4.8:1 to form a mesitylene enrichment liquid (the total content of the two components is more than or equal to 99.5%wt). The tower bottom is a component with the boiling point higher than 165.5 ℃ (namely an aromatic hydrocarbon component with the boiling point higher than that of mesitylene and o-methyl ethylbenzene), the content of mesitylene is lower than 2% (wt), and the heating source is low-pressure steam obtained by flash evaporation of medium-pressure condensate, so that the first heat integration of the invention is formed;
(3) And (3) feeding the tower bottom component of the mesitylene removing tower 5 into the pseudocumene rectifying tower 8 at the speed of 50-80 kmol/h. The top of the column is a mixture of components with boiling points between 165.5 and 169.3 ℃ under the operating conditions of 110-150 kPa.A at a temperature of 180-200 ℃ and a reflux ratio of 10-15:1 (i.e. the components with boiling points between pseudocumene and mesitylene (containing o-methyl ethylbenzene)), and the pseudocumene content is less than 3.5 percent (wt). And (3) extracting the trimellitic product with purity of more than 99% (wt) from the lower part of a side line discharge port, namely the second section of filler, wherein the yield is more than or equal to 91%, and the trimellitic product enters a reboiler of the first light removal tower 2 to serve as a heat source, so that the coupling of the maximum heat of the invention is formed, and the trimellitic product is extracted as a product after the coupling of all latent heat and part of sensible heat are absorbed. The tower kettle is a component with the boiling point higher than 170 ℃, the content of the pseudocumene is lower than 2 percent (wt), and external medium-pressure steam is used as a heat source for heating steam in the tower kettle;
(4) The tower top component of the mesitylene removing tower 5 is sent into the mesitylene extracting and rectifying tower 12 at the speed of 10-15 kmol/h. Under the operation conditions of the tower top pressure of 110-150 kPa.A, the temperature of 170-180 ℃ and the reflux ratio of 10-15:1, a binary mixed solvent of trimethyl trimesic acid and n-octanol is used as an extractant, the molar ratio of trimethyl trimesic acid to n-octanol is 3-5:1, and the molar ratio of the extractant to mesitylene is 8-12:1. The tower top of the extraction rectifying tower is an o-methyl ethylbenzene byproduct which is not absorbed by the solvent, the purity is more than or equal to 98% (wt), and the content of mesitylene is less than 2% (wt). The tower bottom is a mixture of binary extraction solvent and mesitylene, and external medium-pressure steam is used as a heat source for heating steam in the tower bottom;
(5) The tower bottom component of the mesitylene extraction rectifying tower 12 is sent into the mesitylene analyzing tower 15 at the speed of 30-40 kmol/h. Under the operating conditions that the pressure at the top of the tower is 20-50 kPa.A, the temperature is 110-125 ℃ and the reflux ratio is 3-4:1, the purity of the mesitylene product at the top of the tower is more than or equal to 99% (wt), the regenerated binary extraction solvent at the bottom of the tower is recycled to the mesitylene extractive distillation tower 12 for use, and the yield of the mesitylene is more than or equal to 85% (relative to the content in the raw materials, wt);
(6) The tower bottom component of the pseudocumene rectifying tower 8 is fed into a hemimellitene light component removing tower 19 at the speed of 20-30 kmol/h. At an overhead pressure of 2-12 kPa.A, a temperature of 120-140 ℃ and a reflux ratio of 5-8:1, a light component mixture (i.e., a light component between pseudocumene and mesitylene (containing indane, p-methyl cumene)) having a boiling point of between 170 and 176 ℃ is produced at the top of the column, the mesitylene content being less than 2% (wt). The tower bottom is a component with the boiling point higher than 176 ℃ (namely, the component is enriched with the hemimellitene and the carbon nonaromatic hydrocarbon component with the boiling point higher than that of the hemimellitene), and the content of the light component is lower than 0.5 percent (wt);
(7) The bottoms of the hemimellitene light ends column 19 are fed into the hemimellitene removal column 22 at a rate of 15 to 20 kmol/h. Under the operating conditions that the pressure at the top of the tower is 5-10 kPa.A, the temperature is 105-118 ℃ and the reflux ratio is 4-4.8:1, the top of the tower is a mesitylene enrichment liquid formed by mesitylene and p-methyl isopropylbenzene and indane with the boiling point close to the mesitylene, and the total content of the three components is more than or equal to 99.6% (wt). The tower bottom is a component with the boiling point higher than 177.2 ℃ which is a heavy carbon nonaromatic hydrocarbon component as a byproduct, and the content of the hemimellitene is lower than 2 percent (wt);
(8) The overhead components of the deicresylated column 22 are fed to the hemimellitene extractive distillation column 26 at a rate of 8 to 12 kmol/h. Under the operation conditions that the pressure at the top of the tower is 110-150 kPa.A, the temperature is 170-180 ℃ and the reflux ratio is 10-15:1, a binary mixed solvent of 3,4, 5-trimethylphenol and n-octanol is used as an extracting agent, the molar ratio of 3,4, 5-trimethylphenol to n-octanol is 1.5-2.5:1, and the molar ratio of the extracting solvent to mesitylene is 6-8:1; the tower top is p-methyl cumene and indane components which are not absorbed by the solvent, the content of the hemimellitene is less than 2 percent (wt), the tower bottom is a mixture of binary extraction solvent and the hemimellitene, and external medium-pressure steam is used as a heat source for heating steam in the tower bottom;
(9) The bottoms of the hemimellitene extractive rectification column 26 are fed to the hemimellitene column 29 at a rate of 30 to 40 kmol/h. Under the operating conditions that the pressure of the tower top is 10-40 kPa.A, the temperature is 115-135 ℃ and the reflux ratio is 4-6:1, the product of the hemimellitene with the purity more than or equal to 99% (wt) is produced at the tower top, the yield of the hemimellitene is more than or equal to 82% (relative to the content in the raw materials, wt), the tower bottom is the regenerated binary extraction solvent, and the regenerated binary extraction solvent is recycled to the hemimellitene extraction rectifying tower 26 for use.
The method realizes the full separation of the meta-trimethylbenzene, the mesitylene, the hemimellitene and the o-methyl ethylbenzene in the byproduct carbon nine components of the aromatic hydrocarbon combination device of the oil refinery, and the single component with high added value can be purified to the maximum extent.
In a preferred embodiment, in the above step, the pseudocumene rectifying column 8 is operated at a positive pressure, and the refined pseudocumene vapor at the side line of the column can be led back to the reboiler of the first light ends removal column 2 as a heat source to form a first thermal coupling, and then returned to the pseudocumene reflux drum.
In a preferred embodiment, in the above steps, the mesitylene extractive distillation column 12 is operated at positive pressure, and the overhead o-methyl ethylbenzene vapor may be introduced back to the reboiler of the mesitylene removal column 5 as a heat source to form a second thermal coupling, and then returned to the o-methyl ethylbenzene reflux drum.
In a preferred embodiment, in which the hemimellitene extractive distillation column 26 is operated at positive pressure, the overhead indane and methyl cumene vapors may be directed back to the reboiler of the de-hemimellitene column 22 as heat sources to form a third thermal coupling and then back to the reflux drum of the hemimellitene extractive distillation column 26.
In a preferred embodiment, in the step (1), the operation pressure of the column bottom of the first light component removing column 2 is 20 to 24kPa, and the temperature of the column bottom is controlled in the range of 130 to 135 ℃. The aim of such control is that components with boiling points lower than 164.5 ℃ must be removed from the tower kettle components so as to ensure that the mesitylene product is qualified; the operating pressure of the tower top is 12-16 kPa, the control range of the top temperature is 98-105 ℃, and the reflux ratio is 3.2-3.7:1. The purpose of this control is to control the amount of mesitylene removed therefrom to ensure that the overall yield of the desired product is greater than or equal to 85% (wt). The tower kettle heating heat source of the first light component removing tower 2 uses low-pressure steam of a pipe network when the vehicle is started, and the tower top oil gas is led to be used as a heat source after the vehicle is started normally to form thermal coupling.
In a preferred embodiment, in the step (2), the operation pressure of the column bottom of the mesitylene-removing column 5 is 15 to 20kPa, and the temperature of the column bottom is controlled in the range of 135 to 140 ℃. The aim of the control is to remove the components of mesitylene and o-methyl ethylbenzene as much as possible in the components of the tower kettle so as to ensure that the comprehensive yield of the mesitylene target product is more than or equal to 85 percent (wt); the operating pressure of the tower top is 6-8 kPa, the control range of the top temperature is 108-112 ℃, and the reflux ratio is 4.2-4.6:1. The aim of the control is to control the purity of the mesitylene and the o-methyl ethylbenzene in the tower top distillate component to be more than or equal to 99.5 percent so as to ensure that the quality of the mesitylene product is qualified. When a heating source of the tower kettle of the mesitylene removing tower 5 is started, low-pressure steam of a pipe network is used, and after the whole plant is normal, byproduct o-methyl ethylbenzene steam at the tower top of the mesitylene extracting and rectifying tower 12 is used.
In a preferred embodiment, in the step (3), the operating pressure of the column bottom of the pseudocumene rectifying column 8 is 130 to 150kPa, and the temperature of the column bottom is controlled in a range of 195 to 205 ℃. The aim of the control is to remove the component of the pseudocumene as far as possible in the tower kettle component so as to ensure that the comprehensive yield of the pseudocumene product extracted from a liquid collecting disc at the lower part of a second section of packing of the pseudocumene rectifying tower 8 is more than or equal to 91 percent (wt); the operation pressure of the tower top is 120-140 kPa, the control range of the top temperature is 188-195 ℃, and the reflux ratio is 11.5-13.5:1. The purpose of such control is to control the content of the pseudocumene in the overhead component to be less than or equal to 2 percent so as to ensure that the comprehensive yield of the pseudocumene target product is more than or equal to 91 percent (wt).
In a preferred embodiment, in the step (4), the operation pressure of the column bottom of the mesitylene extraction rectifying column 12 is 125 to 140kPa, and the temperature of the column bottom is controlled in the range of 208 to 215 ℃. The aim of the control is to remove the o-methyl-ethylbenzene component as much as possible in the tower kettle component so as to ensure that the quality of the mesitylene product is qualified; the operating pressure of the tower top is 115-130 kPa, the top temperature control range is 172-178 ℃, and the reflux ratio is 14-14.6:1. The purpose of such control is to ensure that the mesitylene content in the o-methyl ethylbenzene product at the top of the tower is less than or equal to 2% (wt) so as to ensure that the comprehensive yield of the mesitylene target product is more than or equal to 85% (wt).
In a preferred embodiment, in the step (5), the operation pressure of the column bottom of the mesitylene analyzing column 15 is 33 to 48kpa.a, and the temperature of the column bottom is controlled in the range of 130 to 145 ℃. The aim of the control is to completely resolve the mesitylene in the extraction solvent so as to ensure that the comprehensive yield of the mesitylene product is more than or equal to 85 percent (wt); the operating pressure of the tower top is 25-40 kPa.A, the control range of the top temperature is 115-120 ℃, and the reflux ratio is 3.2-3.8:1. The purpose of this control is to ensure that the purity of the mesitylene product distilled from the top of the column is not less than 99% (wt).
In a preferred embodiment, in the step (6), the operation pressure of the column bottom of the hemimellitene light ends removal column 19 is 10 to 20kPa, and the temperature of the column bottom is controlled in the range of 140 to 155 ℃. The purpose of such control is that components with boiling points lower than 176 ℃ must be removed from the tower kettle components to ensure that the hemimellitene product is qualified; the operating pressure of the tower top is 5-9 kPa, the control range of the top temperature is 125-135 ℃, and the reflux ratio is 6-7:1. The purpose of this control is to control the amount of mesitylene removed therefrom to ensure a comprehensive yield of the desired product of greater than or equal to 82% (wt).
In a preferred embodiment, in the step (7), the operation pressure of the column bottom of the deimtuzresm column 22 is 15 to 20kPa, and the control temperature of the column bottom is 130 to 140 ℃. The aim of the control is to remove the hemimellitene and the indane and p-methyl isopropylbenzene components with the boiling point very close to that of the hemimellitene as far as possible in the tower kettle component so as to ensure that the comprehensive yield of the hemimellitene target product is more than or equal to 82 percent (wt); the operating pressure of the tower top is 6-8 kPa, the control range of the top temperature is 108-116 ℃, and the reflux ratio is 4.2-4.6:1. The purpose of this control is to control the total content of hemimellitene and indane+p-methyl cumene with very close boiling point in the overhead components to be greater than or equal to 99.6% (wt) to ensure that the quality of the hemimellitene product is acceptable. When the heating source of the tower kettle of the de-trimethyl benzene tower 22 is started, low-pressure steam of a pipe network is used, and after the whole plant is normal, gas phase at the tower top of the de-trimethyl benzene extraction rectifying tower 26 is used.
In a preferred embodiment, in the step (8), the operation pressure of the column bottom of the hemimellitene extractive distillation column 26 is 130 to 150kPa, and the temperature of the column bottom is controlled in the range of 185 to 205 ℃. The aim of the control is to remove indan and p-methyl isopropylbenzene as much as possible in the tower kettle component so as to ensure that the quality of the hemimellitene product is qualified; the operating pressure of the tower top is 120-140 kPa, the top temperature control range is 172-176 ℃, and the reflux ratio is 11-12:1. The purpose of this control is to ensure that the content of the hemimellitene in the overhead product is less than or equal to 2% (wt) so as to ensure that the comprehensive yield of the hemimellitene product is more than or equal to 82% (wt).
In a preferred embodiment, in step (9) above, the operating pressure of the column bottoms of the hemimellitene resolving column 29 is from 25 to 40kpa.a and the kettle temperature control range is from 135 to 150 ℃. The aim of such control is to completely resolve the hemimellitene in the extraction solvent so as to ensure that the comprehensive yield of the hemimellitene product is more than or equal to 82% (wt); the operating pressure of the tower top is 15-30 kPa.A, the control range of the top temperature is 120-130 ℃, and the reflux ratio is 4.5-5.5:1. The purpose of this control is to ensure that the purity of the mesitylene product distilled from the top of the column is not less than 99% (wt).
In specific engineering practice, medium-pressure steam and low-pressure steam condensate are respectively collected according to temperature steps and then used as a multi-stage raw material, a semi-finished product feeding preheating heat source and a heat tracing heat source, so that energy is fully and effectively utilized.
The method provided by the invention ensures that the whole rectification process is safe, efficient, environment-friendly, energy-saving, high in integration level and good in economical efficiency.
The present invention is described in further detail below with reference to specific examples, but is not intended to limit the scope of the present invention.
Example 1
The method comprises the following steps of separating out the o-methyl ethylbenzene as a byproduct of the pseudocumene, the mesitylene and the hemimellitene from the refinery reforming carbon nine-heavy aromatic hydrocarbon raw material:
(1) Feeding a reformed carbon nine-heavy aromatic hydrocarbon raw material from a refinery into a first light component removal tower 2 according to a feeding speed of 10t/h, wherein the operation condition of the first light component removal tower 2 is that the kettle temperature is 133 ℃ and the top temperature is 100 ℃; jacking 15KPa.A; reflux ratio 3.5; the amount of the light component output by the light component conveying pump 3 is 1.65t/h, and the amount of the light component sent to the mesitylene 5 by the conveying pump 4 of the first light component removing tower kettle is 8.35t/h;
(2) The operating conditions of the mesitylene removal column 5 are: the kettle temperature is 138 ℃ and the top temperature is 111 ℃; jacking 7KPa.A; reflux ratio 4.5; the amount of the mesitylene-rich component output by the mesitylene-rich delivery pump 6 to be delivered to the mesitylene extraction rectifying tower 12 is 1.62 t/h; the feeding amount of the component conveying pump 7 of the mesitylene removing tower kettle to the pseudocumene rectifying tower 8 is 6.73t/h;
(3) The operating conditions of the pseudocumene rectifying column 8 are: the kettle temperature is 211 ℃, the top temperature is 192 ℃, and the side draw-out temperature is 190 ℃; jacking 133KPa.A; reflux ratio 12. The amount of the side-stream trimellitic product pumped by the trimellitic product delivery pump 9 is 4.11t/h, the amount of the narrow-fraction aromatic hydrocarbon solvent SA1000# -A output by the component delivery pump 18 with the boiling point of 165.5-169.3 ℃ is 0.86t/h, and the feeding amount of the trimellitic rectifying tower kettle component delivery pump 10 to the hemimellitic light component removal tower 19 is 1.76t/h. The yield of the pseudocumene product is 92.32 percent (wt) calculated by the pseudocumene content in the feed material;
(4) The operating conditions of mesitylene extractive distillation column 12 are: the kettle temperature is 195 ℃ and the top temperature is 175 ℃; jacking 122KPa.A; reflux ratio 14; the molar ratio of trimesic acid trimethyl ester to n-octanol in the extraction solvent is 4:1, and the molar ratio of the extraction solvent to mesitylene is 10:1. The amount of the byproduct o-methyl ethylbenzene product output by the enriched o-methyl ethylbenzene delivery pump 13 is 0.65t/h, and the feeding amount of the component delivery pump 14 of the mesitylene extraction rectifying tower kettle to the mesitylene analyzing tower 15 is 24.18t/h;
(5) The operating conditions of mesitylene column 15 are: the kettle temperature is 140 ℃ and the top temperature is 118 ℃; jacking 30KPa.A; the reflux ratio was 3.5. The amount of the mesitylene product output by the mesitylene product delivery pump 16 is 0.92t/h, and the amount of the extractant delivered to the mesitylene extractive distillation column 12 by the first extractant delivery pump 17 at the bottom of the mesitylene resolution column for recycling is 23.26t/h. The yield of the mesitylene product is 86.71% (wt) calculated by the mesitylene content in the feed raw material;
(6) The operating conditions of the hemimellitene light ends removal tower 19 are that the kettle temperature is 148 ℃ and the top temperature is 130 ℃; pressing 8KPa.A; reflux ratio 6; the amount of light components output by the component conveying pump 20 with the boiling point of 170-176 ℃ is 0.45t/h, and the amount of the components conveyed by the component conveying pump 21 of the light component removing tower kettle of the hemimellitene to be conveyed to the hemimellitene removing tower 22 is 1.31t/h;
(7) The operating conditions of the deironing column 22 are: the kettle temperature is 135 ℃ and the top temperature is 110 ℃; jacking 6KPa.A; reflux ratio 4.6; the amount of the mesitylene-rich component fed to the mesitylene extraction rectifying column 26 from the mesitylene-rich feed pump 23 is 1.05t/h, and the amount of the mesitylene-free column bottom component fed to the storage tank region from the tricresylene-free column bottom component feed pump 24 is 0.26t/h;
(8) The operating conditions of the hemimellitene extractive distillation column 26 are: the kettle temperature is 200 ℃ and the top temperature is 175 ℃; pressing 130KPa.A; reflux ratio 11; the molar ratio of 3,4, 5-trimethylphenol to n-octanol in the extraction solvent is 2:1, and the molar ratio of the extraction solvent to mesitylene is 7:1. The amount of the stream rich in the methyl cumene and the indane outputted by the indane and methyl cumene transfer pump 27 is 0.32t/h, and the amount of the feed of the components of the mesitylene extractive distillation column bottom transfer pump 28 to the mesitylene resolution column 29 is 6.44t/h;
(9) The operating conditions of the hemimellitene column 29 are: the kettle temperature is 145 ℃ and the top temperature is 126 ℃; jacking 20KPa.A; reflux ratio 5. The amount of the mesitylene product output by the mesitylene product transfer pump 30 is 0.71t/h, and the amount of the extraction solvent recycled by the second extractant transfer pump 31 in the mesitylene column bottom to be sent to the mesitylene extractive distillation column 26 is 5.73t/h. The yield of the mesitylene product was 82.35% (wt) calculated on the mesitylene content in the feed material.
(10) Thermal coupling
The first thermal coupling is to introduce the steam at the top of the trimellitic rectifying tower 8 into another reboiler of the first light component removing tower 2 as a heat source, completely release latent heat and partial sensible heat, and return to a reflux tank of the trimellitic rectifying tower 8 after changing into a liquid phase. While the reboiler of the first light ends removal column 2 using low pressure steam as a heat source is completely deactivated, saving 6.35t/h of low pressure steam.
The second thermal coupling is to introduce the steam at the top of the mesitylene extraction rectifying tower 12 into another reboiler of the mesitylene stripping tower 5 to serve as a heat source, completely release latent heat and partial sensible heat, and return to a reflux tank of the mesitylene extraction rectifying tower 12 after being changed into a liquid phase. And the reboiler of the mesitylene removing tower 5 using low-pressure steam as a heat source is completely stopped, so that the low-pressure steam is saved by 3.66t/h.
The third thermal coupling is to introduce the steam at the top of the hemimellitene extractive distillation column 26 into another reboiler of the hemimellitene removal column 22 as a heat source, completely release latent heat and part of sensible heat, and return to the reflux tank of the hemimellitene extractive distillation column 26 after changing into liquid phase. While the reboiler of the deironing column 22 using low pressure steam as the heat source is completely deactivated, saving 2.2t/h of low pressure steam.
(11) Heat integration 1
And (3) completely collecting the medium-pressure condensate, introducing the condensate into a low-pressure steam flash tank, and using the low-pressure steam obtained by flash in a low-pressure steam pipe network.
(12) Heat integration 2
In the industrialized device, the heat exchange between the heated feed and the cooled discharge can reduce the steam consumption and the circulating water consumption. The materials with various temperature levels are gradually heated or cooled according to the temperature steps, and although the process becomes relatively complex and one-time investment is more, the energy saving for long-term operation is quite considerable.
The condensate generated by the low-pressure steam can be reasonably utilized in a gradient mode according to different temperature levels.
The three end products and one by-product obtained were further examined in this example. The detection specifically comprises the following steps:
(1) According to the method specified by the HS/T-2016 national customs industry standard, using Agilent GC-7890 type meteorological chromatograph to respectively measure three final products and one by-product, wherein the specific parameters include: FID detector: 7X 10 -6 mg/ml, PEG-20M capillary column; column temperature: 40 ℃/4 to 80 ℃/8 minutes; rate of temperature rise: 22 ℃/min; vaporization chamber temperature: 188 ℃; split ratio: 120:1, dissolveToluene as the agent;
The final product, pseudocumene, is shown in FIG. 2.
The analysis results were: the purity of the pseudocumene in the final product was 99.32% by weight.
The final mesitylene chromatogram is shown in FIG. 3.
The analysis results were: the mesitylene purity in the final product was 99.09% (wt).
The final product, mesitylene, is shown in figure 4.
The analysis results were: the purity of mesitylene in the final product was 99.16% (wt).
The chromatogram of the by-product o-methyl ethylbenzene is shown in FIG. 5.
The analysis results were: the purity of the by-product o-methyl ethylbenzene was 95.56% (wt).
Example 2
Compared with example 1, the difference is that: the molar ratio of trimesic acid trimethyl ester to n-octanol in the extraction solvent in the step (4) is 3:1.
The three end products and one by-product were tested and the results were:
the purity of the pseudocumene in the final product is 99.29% (wt);
the purity of mesitylene in the final product is 98.63% (wt);
the purity of the mesitylene in the final product is 99.10% (wt);
the purity of the by-product o-methyl ethylbenzene was 93.28% (wt).
Compared with example 1, the mesitylene yield is reduced (relative to the content in the raw materials) to 80.29%, and the reduction is 6.42%; the yield of o-methyl ethylbenzene was reduced (relative to the content of feed) by about 10%.
Example 3
Compared with example 1, the difference is that: the molar ratio of trimesic acid trimethyl ester to n-octanol in the extraction solvent in the step (4) is 5:1.
The three end products and one by-product were tested and the results were:
the purity of the pseudocumene in the final product is 99.25% (wt);
the purity of mesitylene in the final product is 98.68% (wt);
the purity of the mesitylene in the final product is 99.20% (wt);
the purity of the by-product o-methyl ethylbenzene was 95.61% (wt).
Compared with example 1, the mesitylene yield is increased (relative to the content in the raw material) to 86.92%, and the increase is 0.21%; the yield of the o-methyl ethylbenzene increases (relative to the content in the raw material) by about 1%; but the overall plant energy consumption increases by about 6.5%, which is economically a relatively large negative correlation. And the purity of the mesitylene product is reduced to below 99 percent.
Example 4
Compared with example 1, the difference is that: the molar ratio of 3,4, 5-trimethylphenol to n-octanol in the extraction solvent of the step (8) is 1.5:1.
The three end products and one by-product were tested and the results were:
the purity of the pseudocumene in the final product is 99.18% (wt);
the purity of mesitylene in the final product is 99.12% (wt);
the purity of the mesitylene in the final product is 99.21% (wt);
The purity of the by-product o-methyl ethylbenzene was 95.37% (wt).
Compared with example 1, the yield of mesitylene was reduced (relative to the content of the raw material) to 76.54%, by 5.81%, and the amplitude was larger.
Example 5
Compared with example 1, the difference is that: the molar ratio of 3,4, 5-trimethylphenol to n-octanol in the extraction solvent of the step (8) is 2.5:1.
The three end products and one by-product were tested and the results were:
the purity of the pseudocumene in the final product is 99.22% (wt);
the purity of mesitylene in the final product is 99.06% (wt);
the purity of the mesitylene in the final product is 98.39% (wt);
the purity of the by-product o-methyl ethylbenzene was 95.44% (wt).
Compared with example 1, the yield of the hemimellitene is increased (relative to the content of the raw materials) to 83.02 percent, and the increase is 0.67 percent; but the overall plant energy consumption increases by about 5.35% and presents a relatively large negative correlation economically. And the purity of the product is reduced to below 99 percent.
While the invention has been described in detail in the foregoing general description, embodiments and experiments, it will be apparent to those skilled in the art that modifications and improvements can be made thereto. Accordingly, such modifications or improvements may be made without departing from the spirit of the invention and are intended to be within the scope of the invention as claimed.
Claims (8)
1. A process for separating a mixture of carbon nonaarenes, wherein the mixture of carbon nonaarenes comprises pseudocumene, mesitylene and at least one member selected from the group consisting of p-methyl cumene and indane, the process comprising the steps of:
(1) Introducing heavy components with the boiling point higher than 165.5 ℃ in the carbon nona-arene mixture into a pseudocumene rectifying tower, leading out pseudocumene products from the side line of the pseudocumene rectifying tower, leading out light components with the boiling point between 165.5 and 169.3 ℃ from the top of the tower, and leading out heavy components with the boiling point higher than 170 ℃ from the bottom of the tower;
(2) Introducing the heavy component with the boiling point higher than 170 ℃ in the step (1) into a hemimellitene light component removing tower, extracting light components with the boiling point between 170 and 176 ℃ from the top of the hemimellitene light component removing tower, and extracting the heavy component with the boiling point higher than 176 ℃ from the bottom of the tower;
(3) Introducing the heavy component with the boiling point higher than 176 ℃ in the step (2) into a de-trimethyl benzene tower, extracting light components containing the de-trimethyl benzene and at least one of p-methyl cumene and indane from the top of the de-trimethyl benzene tower, and extracting the heavy component with the boiling point higher than 177.2 ℃ from the bottom of the tower;
(4) Introducing the light component in the step (3) into a hemimellitene extractive distillation column, carrying out extractive distillation in the presence of a second extractant, extracting at least one selected from p-methyl isopropylbenzene and indane from the top of the hemimellitene extractive distillation column, and extracting a heavy component containing the second extractant and the hemimellitene from the bottom of the column;
The second extractant is a mixed solution comprising 3,4, 5-trimethylphenol and n-octanol, and the molar ratio of the 3,4, 5-trimethylphenol to the n-octanol is 1.8-2.2:1.
2. The process for separating a mixture of carbon nonaarenes according to claim 1, further comprising the steps of: introducing the heavy component containing the second extractant and the hemimellitene in the step (4) into a hemimellitene resolving tower, leading out the hemimellitene product from the top of the hemimellitene resolving tower, and leading out the second extractant from the bottom of the tower.
3. The process for separating a mixture of carbon nonaaromatics according to claim 1 or 2, further comprising mesitylene and o-methylethylbenzene, said process further comprising the steps of:
(5) Introducing the mixture of the carbon nine aromatic hydrocarbon into a first light component removing tower, extracting light components with boiling point lower than 164.5 ℃ from the top of the first light component removing tower, and extracting heavy components containing mesitylene and o-methyl ethylbenzene from the bottom of the tower;
(6) Introducing the heavy component in the step (5) into a mesitylene removing tower, extracting light components containing mesitylene and o-methyl ethylbenzene from the top of the mesitylene removing tower, and extracting the heavy component with the boiling point higher than 165.5 ℃ from the bottom of the tower;
(7) Introducing the light component containing the mesitylene and the o-methyl ethylbenzene in the step (6) into a mesitylene extraction and rectification tower, carrying out extraction and rectification in the presence of a first extractant, leading out an o-methyl ethylbenzene product from the top of the mesitylene extraction and rectification tower, and leading out heavy component containing the first extractant and the mesitylene from the bottom of the tower;
wherein the first extractant is a mixed solution comprising trimesic acid trimethyl and n-octanol.
4. The method for separating a mixture of carbon nonaarenes according to claim 3, wherein the molar ratio of trimesic acid trimethyl ester to n-octanol is 3-5:1.
5. The method for separating a mixture of carbon nonaarenes according to claim 4, wherein the molar ratio of trimesic acid trimethyl ester to n-octanol is 3.5-4.5:1.
6. The method for separating a mixture of carbon nonaarenes according to claim 5, wherein the molar ratio of trimesic acid trimethyl ester to n-octanol is 3.8-4.2:1.
7. A process for separating a mixture of carbon nonaarenes according to claim 3, further comprising the steps of: introducing the heavy component containing the first extractant and the mesitylene in the step (7) into a mesitylene analysis tower, leading out a mesitylene product from the top of the mesitylene analysis tower, and leading out the first extractant from the tower bottom.
8. A method for separating mesitylene from at least one selected from the group consisting of p-methyl cumene and indane, comprising the steps of: extracting and rectifying a system containing mesitylene and at least one of p-methyl isopropylbenzene and indane in the presence of an extracting agent, wherein the extracting agent is a mixed solution comprising 3,4, 5-trimethylphenol and n-octanol; the molar ratio of the 3,4, 5-trimethylphenol to the n-octanol is 1.8-2.2:1.
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