CN100424055C - Parallel trimethyl benzene separating apparatus and method - Google Patents
Parallel trimethyl benzene separating apparatus and method Download PDFInfo
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- CN100424055C CN100424055C CNB2006101304156A CN200610130415A CN100424055C CN 100424055 C CN100424055 C CN 100424055C CN B2006101304156 A CNB2006101304156 A CN B2006101304156A CN 200610130415 A CN200610130415 A CN 200610130415A CN 100424055 C CN100424055 C CN 100424055C
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Abstract
The present invention relates to parallel trimethyl benzene separating apparatus and method. The parallel trimethyl benzene separating apparatus includes a pre-separating tower, a sym-trimethyl benzene tower and an unsym-trimethyl benzene tower, and features the vacuum unit on the pre-separating tower, the condensator connected to the outlet of the pre-separating tower, the reflux accumulator connected to connected to the inlet of the sym-trimethyl benzene tower, the reboiler in the bottom of the pre-separating tower connected between the outlet and the inlet of the sym-trimethyl benzene tower. The present invention adopts a parallel three-tower process, can produce unsym-trimethyl benzene in purity over 99 % in the yield over 90 % and sym-trimethyl benzene in purity over 35 % simultaneously in the yield over 85 % and power consumption 30 %-40 % lower than one normal pressure process.
Description
Technical field
The present invention relates to the fine chemistry industry separation technology field, specifically is parallel trimethyl benzene separating apparatus and method.
Background technology
Carbon such as trimethylbenzene nine heavy aromaticss mainly come from refinery's reformer, and wherein unsym-trimethyl benzene and sym-trimethylbenzene are important fine chemical products, have very high added value.Wherein unsym-trimethyl benzene is of many uses as basic Organic Chemicals, is mainly used to isomerization and produces sym-trimethylbenzene, synthetic trimellitic acid 1,2-anhydride.With the enriched mesitylene is raw material, carries out catalytic alkylation reaction, can obtain the high purity sym-trimethylbenzene, and sym-trimethylbenzene can be used to produce 2,4,6-trimethylaniline, also can make dyestuff intermediate etc.
Domestic trimethylbenzene separation process adopts the normal pressure double-column process mostly, only produces unsym-trimethyl benzene, and a large amount of valuable sym-trimethylbenzene are used to do gasoline dope.Adopt three-column process flow under normal pressure, energy consumption is bigger, influences economic benefit.This is because each component of C9 aromatic hydrocarbons in the charging is a series of isomerss, boiling-point difference is little each other, want isolating sym-trimethylbenzene to have very much the component o-methylethylbenzene between the unsym-trimethyl benzene, wherein unsym-trimethyl benzene and o-methylethylbenzene boiling-point difference are 4.2 ℃, 0.5 ℃ of sym-trimethylbenzene and o-methylethylbenzene boiling-point difference, separating difficulty is big, and required each tower number of theoretical plate is more, and therefore the investment and the process cost of device are all higher.
Summary of the invention
Purpose of the present invention, provide a kind of trimethylbenzene separation method that cuts down the consumption of energy, it adopts raw material after presorting tower, the separating technology that sym-trimethylbenzene tower and unsym-trimethyl benzene tower are parallel, presort tower and adopt negative-pressure operation, the sym-trimethylbenzene tower adopts normal pressure or pressurized operation, in production high purity unsym-trimethyl benzene, and the coproduction enriched mesitylene.Three towers all adopt Sulzer packing, and Ta Nei establishes many rounds full-mesh sparger, can reduce the rectifying tower height, increase turndown ratio.
Technology of the present invention is as follows:
Parallel trimethyl benzene separating apparatus of the present invention comprises through presorting tower 1, sym-trimethylbenzene tower 2 and unsym-trimethyl benzene tower 3; It is characterized in that presorting tower and be provided with vacuum unit 8, presort tower top outlet and connect condenser 6, return tank 7 successively, be connected through pipeline with sym-trimethylbenzene tower opening for feed; Presort the outlet of bottoms material and be connected, presort tower bottom reboiler 9 two ends and be connected with import with the sym-trimethylbenzene tower top outlet respectively with unsym-trimethyl benzene tower 3 opening for feeds; The unsym-trimethyl benzene tower is provided with condenser, reboiler.
Presort tower, sym-trimethylbenzene tower and unsym-trimethyl benzene tower of the present invention all adopt Sulzer packing, and Ta Nei establishes many rounds full-mesh sparger.
The working method of parallel trimethyl benzene separating apparatus of the present invention is: adopt the parallel trimethyl benzene separation method: C9 aromatic raw material 4 is after interchanger 5 heat exchange, enter and presort tower 1, it is presorted tower and adopts negative-pressure operation, cat head connects vacuum unit 8, the cat head gas phase enters return tank 7 behind condenser 6, phlegma partial reflux wherein, part is as 2 chargings of sym-trimethylbenzene tower, the bottoms material enters unsym-trimethyl benzene tower 3, and the most of gas phase of the cat head of sym-trimethylbenzene tower realizes thermal coupling as the thermal source of presorting tower bottom reboiler 9, a cat head gaseous condensate part refluxes, a part of as lightnaphtha A extraction, extraction enriched mesitylene product B at the bottom of the tower, its unsym-trimethyl benzene cat head gas phase is through condenser 12, enter return tank 13, part phlegma refluxes, and another part phlegma is as the extraction of unsym-trimethyl benzene products C, extraction heavy naptha D at the bottom of the tower.
The described pressure tower of presorting is controlled at 30～70KPa, and tower top temperature is controlled at 100～180 ℃.
Described sym-trimethylbenzene pressure tower is controlled at 100～200KPa, and tower top temperature is controlled at 120～200 ℃.
Advantage of the present invention is:
(1) adopt raw material after presorting tower, the separation process that sym-trimethylbenzene tower and unsym-trimethyl benzene tower are parallel, the enriched mesitylene of coproduction more than 35% in the unsym-trimethyl benzene of production purity more than 99%, wherein the yield of unsym-trimethyl benzene is all more than 90%, and the yield of sym-trimethylbenzene is all more than 85%.
(2) adopt the differential pressure operation, the sym-trimethylbenzene tower adopts normal pressure or pressurization, presort tower and adopt decompression, with the cat head gas phase that reaches equal toluene tower as the thermal source of presorting tower bottom reboiler, the realization thermal coupling.
(3) compare with the normal pressure flow process, unit consumption of energy can reduce by 30%～40%.
(4) three towers all adopt wavy metal net filler, and Ta Nei establishes many rounds full-mesh sparger.
Description of drawings
Fig. 1 is a schema of the present invention:
Wherein: 1 for presorting tower, and 2 is the sym-trimethylbenzene tower, and 3 is the unsym-trimethyl benzene tower, 4 is the C9 aromatic feed, and 5 is interchanger, and 6 for presorting overhead condenser, 7 is return tank, and 8 is vacuum unit, and 9 for presorting tower bottom reboiler, 10 is unsym-trimethyl benzene tower fresh feed pump, and 11 is the sym-trimethylbenzene tower bottom reboiler, and 12 is the unsym-trimethyl benzene overhead condenser, 13 is the unsym-trimethyl benzene return tank of top of the tower, and 14 is the unsym-trimethyl benzene tower bottom reboiler, and A is a lightnaphtha, B is an enriched mesitylene, and C is a unsym-trimethyl benzene, and D is a heavy oil.
Embodiment
Embodiment 1
Presort tower, sym-trimethylbenzene tower and unsym-trimethyl benzene tower and all adopt Sulzer packing, Ta Nei establishes many rounds full-mesh sparger.C9 aromatic raw material 4 is after interchanger 5 heat exchange, enter and presort tower 1, it is presorted tower and adopts the 30KPa operation, tower top temperature is controlled at more than 100 ℃, cat head connects vacuum unit 8, and the cat head gas phase enters return tank 7, wherein phlegma partial reflux behind condenser 6, part is as 2 chargings of sym-trimethylbenzene tower, and the bottoms material enters unsym-trimethyl benzene tower 3.The sym-trimethylbenzene pressure tower is controlled at about 100KPa, tower top temperature is controlled at more than 120 ℃, make the most of gas phase of cat head as the thermal source of presorting tower bottom reboiler 9, realize thermal coupling, a cat head gaseous condensate part refluxes, a part of as lightnaphtha A extraction, extraction enriched mesitylene product B at the bottom of the tower.Unsym-trimethyl benzene cat head gas phase enters return tank 13 through condenser 12, and a part of phlegma refluxes, and another part phlegma is as the extraction of unsym-trimethyl benzene products C, extraction heavy naptha D at the bottom of the tower.Gained unsym-trimethyl benzene purity reaches 99%, and yield is more than 90%, sym-trimethylbenzene purity 35%, and yield reaches 85%.
Embodiment 2
Presort tower, sym-trimethylbenzene tower and unsym-trimethyl benzene tower and all adopt Sulzer packing, Ta Nei establishes many rounds full-mesh sparger.C9 aromatic raw material 4 is after interchanger 5 heat exchange, enter and presort tower 1, it is presorted tower and adopts the 50KPa operation, tower top temperature is controlled at about 140 ℃, and cat head connects vacuum unit 8, and the cat head gas phase enters return tank 7 behind condenser 6, phlegma partial reflux wherein,, part is as 2 chargings of sym-trimethylbenzene tower, and the bottoms material enters unsym-trimethyl benzene tower 3.The sym-trimethylbenzene pressure tower is controlled at about 150KPa, tower top temperature is controlled at about 170 ℃, make the most of gas phase of cat head as the thermal source of presorting tower bottom reboiler 9, realize thermal coupling, a cat head gaseous condensate part refluxes, a part of as lightnaphtha A extraction, extraction enriched mesitylene product B at the bottom of the tower.Unsym-trimethyl benzene cat head gas phase enters return tank 13 through condenser 12, and a part of phlegma refluxes, and another part phlegma is as the extraction of unsym-trimethyl benzene products C, extraction heavy naptha D at the bottom of the tower.Gained unsym-trimethyl benzene purity reaches 99%, and yield is more than 90%, sym-trimethylbenzene purity 35%, and yield reaches 85%.
Embodiment 3
Presort tower, sym-trimethylbenzene tower and unsym-trimethyl benzene tower and all adopt Sulzer packing, Ta Nei establishes many rounds full-mesh sparger.C9 aromatic raw material 4 is after interchanger 5 heat exchange, enter and presort tower 1, it is presorted tower and adopts the 80KPa operation, tower top temperature is controlled at below 180 ℃, and cat head connects vacuum unit 8, and the cat head gas phase enters return tank 7 behind condenser 6, phlegma partial reflux wherein,, part is as 2 chargings of sym-trimethylbenzene tower, and the bottoms material enters unsym-trimethyl benzene tower 3.The sym-trimethylbenzene pressure tower is controlled at about 200KPa, tower top temperature is controlled in 200 ℃, make the most of gas phase of cat head as the thermal source of presorting tower bottom reboiler 9, realize thermal coupling, a cat head gaseous condensate part refluxes, a part of as lightnaphtha A extraction, extraction enriched mesitylene product B at the bottom of the tower.Unsym-trimethyl benzene cat head gas phase enters return tank 13 through condenser 12, and a part of phlegma refluxes, and another part phlegma is as the extraction of unsym-trimethyl benzene products C, extraction heavy naptha D at the bottom of the tower.Gained unsym-trimethyl benzene purity reaches 99%, and yield is more than 90%, sym-trimethylbenzene purity 35%, and yield reaches 85%.
Parallel trimethyl benzene separating apparatus and method that the present invention proposes, be described by embodiment, person skilled obviously can be changed or suitably change and combination content as herein described in not breaking away from content of the present invention, spirit and scope, realizes the present invention.Special needs to be pointed out is, the replacement that all are similar and change apparent to those skilled in the artly, they are regarded as being included in the utility model spirit, scope and the content.
Claims (5)
1. a parallel trimethyl benzene separating apparatus comprises and presorts tower (1), sym-trimethylbenzene tower (2) and unsym-trimethyl benzene tower (3); It is characterized in that presorting tower and be provided with vacuum unit (8), presort tower top outlet and connect condenser (6), return tank (7) successively, be connected through pipeline with sym-trimethylbenzene tower opening for feed; Presort the outlet of bottoms material and be connected, presort tower bottom reboiler (9) two ends and be connected with import with the sym-trimethylbenzene tower top outlet respectively with unsym-trimethyl benzene tower (3) opening for feed; The unsym-trimethyl benzene tower is provided with condenser and reboiler.
2. parallel trimethyl benzene separating apparatus as claimed in claim 1 is characterized in that the described employing Sulzer packing in tower, sym-trimethylbenzene tower and the unsym-trimethyl benzene tower of presorting, and Ta Nei establishes many rounds full-mesh sparger.
3. the working method of parallel trimethyl benzene separating apparatus as claimed in claim 1, it is characterized in that C9 aromatic raw material (4) is after interchanger (5) heat exchange, enter and presort tower (1), it is presorted tower and adopts negative-pressure operation, cat head connects vacuum unit (8), the cat head gas phase enters return tank (7) behind condenser (6), phlegma partial reflux wherein, part is as sym-trimethylbenzene tower (2) charging, the bottoms material enters unsym-trimethyl benzene tower (3), the most of gas phase of the cat head of sym-trimethylbenzene tower is as presorting the thermal source of tower bottom reboiler (9), realize thermal coupling, a cat head gaseous condensate part refluxes, and a part is as lightnaphtha (A) extraction, extraction enriched mesitylene product (B) at the bottom of the tower, its unsym-trimethyl benzene cat head gas phase enters return tank (13) through condenser (12), and a part of phlegma refluxes, another part phlegma is as unsym-trimethyl benzene product (C) extraction, extraction heavy naptha (D) at the bottom of the tower.
4. the working method of parallel trimethyl benzene separating apparatus as claimed in claim 3 is characterized in that the described pressure tower of presorting is controlled at 30～70KPa, and tower top temperature is controlled at 100～180 ℃.
5. the working method of parallel trimethyl benzene separating apparatus as claimed in claim 3 is characterized in that described sym-trimethylbenzene pressure tower is controlled at 100～200KPa, and tower top temperature is controlled at 120～200 ℃.
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| CNB2006101304156A CN100424055C (en) | 2006-12-20 | 2006-12-20 | Parallel trimethyl benzene separating apparatus and method |
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| CNB2006101304156A CN100424055C (en) | 2006-12-20 | 2006-12-20 | Parallel trimethyl benzene separating apparatus and method |
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| CN100424055C true CN100424055C (en) | 2008-10-08 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| ITPI20100114A1 (en) * | 2010-10-11 | 2012-04-12 | Sime S R L | EQUIPMENT AND PROCESS FOR SEPARATING 1,2,4 TRIMETHYLBENZENE (PSEUDOCUMENE) FROM A MIXTURE CONTAINING AROMATIC HYDROCARBONS |
Families Citing this family (5)
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| CN101723790B (en) * | 2008-10-30 | 2013-05-01 | 中国石油化工股份有限公司 | Method for separating mixture of m-ethyltoluene and o-ethyltoluene from C9 aromatics |
| CN101723791B (en) * | 2008-10-30 | 2013-05-01 | 中国石油化工股份有限公司 | Method for enriching mesitylene from C9 aromatics |
| CN102580338B (en) * | 2012-02-23 | 2014-04-16 | 淄博市临淄齐泉工贸有限公司 | Method for continuously rectifying 3-chloropropyl triethoxysilane |
| CN107050912B (en) * | 2017-01-13 | 2022-08-02 | 陕西延长石油（集团）有限责任公司 | Gas-phase condensed liquid recovery system and method |
| CN111569458A (en) * | 2020-06-10 | 2020-08-25 | 安庆亿成化工科技有限公司 | Meta-trimethylbenzene rectifying device and method based on thermal coupling process |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| ITPI20100114A1 (en) * | 2010-10-11 | 2012-04-12 | Sime S R L | EQUIPMENT AND PROCESS FOR SEPARATING 1,2,4 TRIMETHYLBENZENE (PSEUDOCUMENE) FROM A MIXTURE CONTAINING AROMATIC HYDROCARBONS |
| WO2012056278A2 (en) | 2010-10-11 | 2012-05-03 | Sime Srl | Process and equipment for separating 1,2,4 trimethylbenzene (pseudocumene) from a mixture containing aromatic hydrocarbons |
| WO2012056278A3 (en) * | 2010-10-11 | 2012-11-15 | Sime Srl | Process and equipment for separating 1,2,4 trimethylbenzene (pseudocumene) from a mixture containing aromatic hydrocarbons |
| US9550133B2 (en) | 2010-10-11 | 2017-01-24 | Sime Srl | Process and equipment for separating 1,2,4 trimethylbenzene (pseudocumene) from a mixture containing aromatic hydrocarbons |
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