CN102372576B - Method for separating m-methylethylbenzene and p-methylethylbenzene mixture from C9 aromatic hydrocarbon - Google Patents
Method for separating m-methylethylbenzene and p-methylethylbenzene mixture from C9 aromatic hydrocarbon Download PDFInfo
- Publication number
- CN102372576B CN102372576B CN 201010257340 CN201010257340A CN102372576B CN 102372576 B CN102372576 B CN 102372576B CN 201010257340 CN201010257340 CN 201010257340 CN 201010257340 A CN201010257340 A CN 201010257340A CN 102372576 B CN102372576 B CN 102372576B
- Authority
- CN
- China
- Prior art keywords
- tower
- agent
- methyl
- ethylbenzene
- mixture
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a method for separating an m-methylethylbenzene and p-methylethylbenzene mixture from C9 aromatic hydrocarbon. An accelerator is added in the rectification process and is one of acetonitrile and propionitrile. The method comprises the following steps of: (1) mixing a C9 aromatic hydrocarbon mixture and the accelerator, leading into a light component removal tower, leading out light components from the top of the light component removal tower, and leading out heavy components from the tower; (2) leading the light components obtained in step (1) into a first accelerator removal tower, leading out the accelerator from the top of the tower, and leading out light component material flow from the tower; (3) mixing the heavy components obtained in step (1) and the accelerator, leading into a heavy component removal tower, and leading out material flow from the top of the tower and the tower respectively; and (4) leading the material flow which is obtained in step (3) and is lead out from the top of the heavy component removal tower into a second accelerator removal tower, leading out the accelerator from the top of the tower, and leading out the m-methylethylbenzene and p-methylethylbenzene mixture from the tower. The m-methylethylbenzene and p-methylethylbenzene mixture obtained by the method has high purity, is high in yield and has a remarkable separation effect.
Description
Technical field
The present invention relates to organic chemistry filed, say further, relate to a kind of from C9 aromatic the method for compartment, p-methyl-ethylbenzene mixture.
Background technology
The exploitation of C9 aromatic deep processing technology and the utilization of various components are the problems that people are concerned about always.The composition of different chemical-process by-product C9 aromatic cuts is different, and its basal component such as sym-trimethylbenzene, unsym-trimethyl benzene, first and second benzene etc. all are the important chemical resources.First and second benzene comprise the neighbour,, to three kinds of isomer, proportion is higher in the C9 aromatic mixture, especially can account for 25%-30% in reformation C9 aromatic cut.Because boiling-point difference only is 0.7 ℃ between m-methyl ethylbenzene and the p-methyl-ethylbenzene, be difficult to disposablely separate fully, so C9 aromatic separate and mostly be between, the p-methyl-ethylbenzene mixture.
CN1958538A discloses a kind of method of separating C9 aromatic, comprise the C9 aromatic mixture is carried out prefractionation, intercepting contains the enriched fraction of sym-trimethylbenzene and o-methylethylbenzene, and by-product contains n-proplbenzene, isopropyl benzene simultaneously,, low boiling mixture product and the unsym-trimethyl benzene product of p-methyl-ethylbenzene; The enriched fraction that will contain sym-trimethylbenzene and o-methylethylbenzene is introduced the double solvent extraction rectifying tower, under solvent pairs synergistic extraction effect, obtains sym-trimethylbenzene product and o-methylethylbenzene product.Wherein said prefractionation step can adopt precise distillation or extracting rectifying, and when adopting precise distillation technology, stage number could effectively be separated sym-trimethylbenzene greater than 200, obtain just the containing of higher yields, isopropyl benzene between, the mixture of p-methyl-ethylbenzene.How this technology does not relate to and further just separating, isopropyl benzene, obtain high purity (greater than 95%) more between, the p-methyl-ethylbenzene mixture.
(print during chemical industry in the literature, the 2nd phase of calendar year 2001, P.25) in the author to adopt number of theoretical plate be the experiment that 60 glass filler tower has carried out precision fractional distillation compartment, p-methyl-ethylbenzene mixture, be to carry out precise distillation under the condition of 20-40 in reflux ratio, can obtain purity greater than between 95%, p-methyl-ethylbenzene and o-methylethylbenzene, but the author do not provide from, the p-methyl-ethylbenzene mixture just removing, the experimental data of isopropyl benzene and, the yield of p-methyl-ethylbenzene mixture.
Chinese patent 200810225604.O discloses a kind of method of separating C9 aromatic.These method two tower separation process, weight-removing column pressurized operation, lightness-removing column decompression operation.The method of this invention only improves the weight-removing column working pressure on the existing technology basis of change hardly, reduce the lightness-removing column working pressure, but energy efficient not only, and obtain between, purity and the yield of p-methyl-ethylbenzene mixture compare with existing technology slightly and improve.Owing to adopt the precise distillation method, separate required rectifying tower stage number still more (〉=120), reflux ratio height (〉=35), energy consumption is still quite high, and yield is lower, and quality product is relatively poor.
Because between, the p-methyl-ethylbenzene mixture serves many purposes, as between its dehydrogenation product, p-methylstyrene mixture purposes is very extensive, can carry out copolymerization, composite adhesives, resin, printing ink, dry cleaning composition, coating etc. with multiple the 3rd different monomer respectively; Under catalyst action, it is oxidable to be tolyl acid, and hydrogenation generates the ethyl cyclohexylenedinitrilotetraacetic acid, is applied in siccative, wood preservative, synthetic detergent and the agrochemical aspect of paint.Can therefore, rationally make good use of this part resource of first and second benzene, be especially a reform key factor of C9 aromatic comprehensive utilization of C9 aromatic.
In order to solve the existing problem that from the C9 aromatic raw material, exists in compartment, the p-methyl-ethylbenzene mixture technology, provide a kind of economy, separate obtain between high purity and high yield, the method for p-methyl-ethylbenzene product is very necessary.
Summary of the invention
Be to solve problems of the prior art, the invention provides a kind of from C9 aromatic the method for compartment, p-methyl-ethylbenzene mixture.Have compartment, p-methyl-ethylbenzene mixture purity height and the good advantage of yield.
The purpose of this invention is to provide a kind of from C9 aromatic the method for compartment, p-methyl-ethylbenzene mixture.
When adopting the rectification method separating mixture, the liquid-vaqor interface of system is very big in the rectifying tower, vapour in the rectifying, the mass transfer of liquid two-phase carries out in liquid-vaqor interface, the quality of the effect of separation mixture, the vapour phase that not only depends on system, the thermodynamic property of liquid phase and the rule of stream-liquid phase balance, but also the surface properties that depends on liquid and various components break away from speed speed different of vapour phase from fluid surface, therefore, can use to increase the relative volatility that desire is separated the purpose component, can make purpose component faster disengaging roll body surface again and the special extract rectification method of transferring to vapour phase realizes the separation of the system that boiling point is close very much.In order to achieve the above object, in rectifying tower, add a kind of special solvent, the adding of this special solvent has not only increased desire and has separated the relative volatility that the purpose component divides, and the purpose component is shifted quickly to vapour phase from liquid phase than other component, above-mentioned special extract rectification method is named as benzene with catalytic rectifying method, and used special solvent claims to urge agent.
In general, urge the selection of agent mainly to take all factors into consideration from the following aspects:
(1) urges agent to separate the purpose component with desire bigger seemingly avidity and bigger surfactivity are arranged;
(2) urge agent not with raw material in any component generation chemical reaction, do not form azeotrope yet;
(3) urge the agent boiling point low than each component boiling point in the raw material, can recycle by conventional distillation;
(4) urge agent and separated component intermiscibility better, avoid taking place demixing phenomenon;
(5) urge agent to want nontoxic or hypotoxicity, non-corrosiveness, Heat stability is good and cheap, obtain easily.
What the present invention adopted is exactly above-described benzene with catalytic rectifying method, adds in rectifying that to urge agent, described urgency agent be a kind of in acetonitrile and the propionitrile, preferred propionitrile.
Described method comprises following steps:
(1) introduces lightness-removing column with the C9 aromatic mixture with after urging agent to mix, draw the light constituent that comprises n-proplbenzene, isopropyl benzene and urgency agent by the lightness-removing column top, drawn the heavy constituent that contain m-methyl ethylbenzene, p-methyl-ethylbenzene, sym-trimethylbenzene, o-methylethylbenzene, unsym-trimethyl benzene and hemimellitene by the lightness-removing column still
Wherein said C9 aromatic mixture is 1: 0.01～0.5 with the weight ratio of urging agent, be preferably 1: 0.05～and 0.3, more preferably 1: 0.05～0.1;
(2) light constituent described in the step (1) is introduced first and taken off urgency agent tower, take off by first and urge the agent cat head to draw the urgency agent, take off by first and urge the agent tower reactor to draw the light constituent logistics that contains n-proplbenzene, isopropyl benzene;
(3) introduce weight-removing column with heavy constituent described in the step (1) with after urging agent to mix, draw the logistics that comprises m-methyl ethylbenzene, p-methyl-ethylbenzene and urgency agent by the weight-removing column top, drawn the component that contains sym-trimethylbenzene, o-methylethylbenzene, unsym-trimethyl benzene and hemimellitene by the weight-removing column still
Wherein said heavy constituent are 1: 0.01～0.5 with the weight ratio of urging agent, be preferably 1: 0.05～and 0.3, more preferably 1: 0.05～0.1;
(4) logistics that the weight-removing column described in the step (3) top is drawn is introduced second and is taken off and urge the agent tower, take off by second and urge the agent cat head to draw the urgency agent, by second take off urge the agent tower reactor draw between, the p-methyl-ethylbenzene mixture.
The equipment of using in the method for the invention is the equipment that adopts usually in the C9 aromatic rectifying as lightness-removing column, weight-removing column.
In the concrete operations, can implement by following condition:
The stage number of described lightness-removing column is 30～100, and tower top temperature is 80～170 ℃, and tower top pressure is 0.1～0.5MPa, and the tower reactor temperature is 170～210 ℃, and tower reactor pressure is 0.12～0.8MPa, and reflux ratio is 5～20; Preferably: the stage number of lightness-removing column is 50～70, and tower top temperature is 90～160 ℃, and tower top pressure is 0.1～0.3MPa, and the tower reactor temperature is 175～190 ℃, and tower reactor pressure is 0.12～0.4MPa, and reflux ratio is 7～14;
Described first stage number of taking off urgency agent tower is 5～20, and tower top temperature is 80～140 ℃, and tower top pressure is 0.1～0.5MPa, and the tower reactor temperature is 150～190 ℃, and tower reactor pressure is 0.11～0.8MPa, and reflux ratio is 2～15; Preferably: first stage number of taking off urgency agent tower is 8～15, and tower top temperature is 80～120 ℃, and tower top pressure is 0.1～0.3MPa, and the tower reactor temperature is 155～170 ℃, and tower reactor pressure is 0.11～0.4MPa, and reflux ratio is 2～5;
The stage number of described weight-removing column is 30～90, and tower top temperature is 80～180 ℃, and tower top pressure is 0.1～0.5MPa, and the tower reactor temperature is 170～210 ℃, and tower reactor pressure is 0.12～0.8MPa, and reflux ratio is 5～20; Preferably: the stage number of weight-removing column is 40～60, and tower top temperature is 90～160 ℃, and tower top pressure is 0.1～0.3MPa, and the tower reactor temperature is 175～190 ℃, and tower reactor pressure is 0.12～0.4MPa, and reflux ratio is 7～12;
Described second stage number of taking off urgency agent tower is 5～20, tower top temperature is 80～140 ℃, and tower top pressure is 0.1～0.5MPa, and the tower reactor temperature is 150～190 ℃, tower reactor pressure is 0.11～0.8MPa, reflux ratio is 2～15, and is preferred: second stage number of taking off urgency agent tower is 8～15, and tower top temperature is 80～120 ℃, tower top pressure is 0.1～0.3MPa, the tower reactor temperature is 155～170 ℃, and tower reactor pressure is 0.11～0.4MPa, and reflux ratio is 2～5.
C9 aromatic mixture of the present invention can be from oil, xylene isomerization by-product at the bottom of the platinum reforming tower, and preferred wherein content middle, p-methyl-ethylbenzene is 15～40 weight %.The C9 aromatic of different sources is formed slightly different, and those skilled in the art can regulate the operating procedure condition according to practical situation.
Method of the present invention has the following advantages:
1, adopt of the present invention from C9 aromatic the stage number of the required rectifying tower of compartment, p-methyl-ethylbenzene mixture method the chances are rectification method separates required tower stage number 1/2, from the data on reflux ratio one hurdle more as can be known, of the present invention from C9 aromatic the productivity (output/hour) of compartment, p-methyl-ethylbenzene mixture be about 4 times of rectification method, urgency agent part in the deduction distillate, and with between distillating, the p-methyl-ethylbenzene mixture calculates, its productivity is about 3.5 times of productivity of rectification method, can reach less investment, aim of high yield.
2, from table 7 data as can be known, adopt method of the present invention, between obtaining, p-methyl-ethylbenzene mixture purity and yield be significantly improved, and can reach high-quality, aim of high yield.
Description of drawings
Fig. 1 of the present invention from C9 aromatic the schematic flow sheet of compartment, p-methyl-ethylbenzene mixture
Description of reference numerals
A1 first mixing tank, A2 second mixing tank, B1 lightness-removing column, B2 weight-removing column, C1 first take off urges agent tower, C2 second to take off urgency agent tower, D1 first condenser, D2 second condenser, D3 the 3rd condenser, D4 the 4th condenser, E1 first return tank, E2 second return tank, E3 the 3rd return tank, E4 the 4th return tank, F1 first reboiler, F2 second reboiler, F3 the 3rd reboiler, F4 the 4th reboiler
Logistics class: 1 C9 aromatic raw material, 2 replenish fresh urgency agent, agent is urged in 3 circulations, 4 contain urgency agent and C9 aromatic raw material, 5 contain n-proplbenzene, the component of isopropyl benzene and urgency agent, 6, contain m-methyl ethylbenzene, p-methyl-ethylbenzene, sym-trimethylbenzene, o-methylethylbenzene, the component of unsym-trimethyl benzene and hemimellitene, 7 contain n-proplbenzene, the light constituent of isopropyl benzene, 8, contain sym-trimethylbenzene, o-methylethylbenzene, the component of unsym-trimethyl benzene and hemimellitene, 9 m-methyl ethylbenzenes, the p-methyl-ethylbenzene mixture, 10 comprise m-methyl ethylbenzene, the component of p-methyl-ethylbenzene and urgency agent, 11 contain urgency agent and m-methyl ethylbenzene, p-methyl-ethylbenzene, sym-trimethylbenzene, o-methylethylbenzene, the component of unsym-trimethyl benzene and hemimellitene
Embodiment
Below in conjunction with embodiment, further specify the present invention.
Below in conjunction with Fig. 1 further describe of the present invention from C9 aromatic the method for compartment, p-methyl-ethylbenzene mixture.
In the first mixing tank A1, enter the middle and lower part of lightness-removing column B1 after urging agent and C9 aromatic raw material 1 to mix, cat head distillates and comprises n-proplbenzene, the light constituent logistics 5 of isopropyl benzene and urgency agent, after first water cooler D1 cooling, enter the cat head first return tank E1, a part is through flowing into the cat head of lightness-removing column B1 as refluxing, a part enters first and takes off the middle and lower part of urging agent tower C1, distillate the urgency agent that recycles in this column overhead, after second water cooler D2 cooling, enter the cat head second return tank E2, a part is taken off the cat head of urging agent tower C1 through flowing into first as refluxing, a part enters the first mixing tank A1 and recycles, and first take off and urge agent tower C1 tower reactor to flow out part containing n-proplbenzene, the logistics 7 of the light constituent of isopropyl benzene, part 7 is returned first and is taken off urgency agent tower C1 after the tower reactor second reboiler F2 boils again; Logistics 6 from the outflow of lightness-removing column B1 tower reactor, contain m-methyl ethylbenzene, p-methyl-ethylbenzene, sym-trimethylbenzene, o-methylethylbenzene, unsym-trimethyl benzene and the logistics of hemimellitene component, part 6 is after the tower reactor first reboiler F1 boils again, return lightness-removing column B1, part 6 is introduced the second mixing tank A2, urge agent to mix the laggard middle and lower part of going into to flow into weight-removing column B2 with circulation, cat head distillates steam 10,10 comprise m-methyl ethylbenzene, the logistics of p-methyl-ethylbenzene and urgency agent, after the 3rd water cooler D3 cooling, enter cat head the 3rd return tank E3, a part flows into the cat head of weight-removing column B2 as refluxing, a part enters second and takes off the middle and lower part of urging agent tower C2, distillate the urgency agent that recycles in this column overhead, after the 4th water cooler D4 cooling, enter cat head the 4th return tank E4, a part is taken off the cat head of urging agent tower C2 through flowing into second as refluxing, a part enters the second mixing tank A2 and recycles, and second take off and urge agent tower C2 tower reactor to isolate containing m-methyl ethylbenzene, p-methyl-ethylbenzene mixture stream passes 9, part 9 is returned second and is taken off urgency agent tower C2 after tower reactor the 4th reboiler F4 boils again; Logistics 8 from weight-removing column B2 tower reactor flows out contains the logistics of sym-trimethylbenzene, o-methylethylbenzene, unsym-trimethyl benzene and hemimellitene component, and part 8 is returned weight-removing column B2 after tower reactor the 3rd reboiler F3 boils again, and part is drawn.
Embodiment 1～6
By above-described from C9 aromatic the method for compartment, p-methyl-ethylbenzene implement, concrete processing condition, parameter and used urgency agent see Table 2～table 4.
Used in an embodiment of the present invention carbon nine C9 aromatic hydrocarbons mixtures are reformation C9 aromatic cuts, wherein contain approximately 23% (weight) between, p-methyl-ethylbenzene, its concrete component and content see Table 1.
Composition and the boiling point of table 1 C9 aromatic raw material
| The component title | Content (weight %) | Boiling point (℃) |
| P-Xylol | 0.30 | 138.4 |
| Isopropyl benzene | 0.46 | 152.2 |
| N-proplbenzene | 4.54 | 159.20 |
| M-methyl ethylbenzene | 16.80 | 161.33 |
| P-methyl-ethylbenzene | 6.13 | 162.01 |
| Sym-trimethylbenzene | 6.81 | 164.74 |
| O-methylethylbenzene | 7.61 | 165.18 |
| Unsym-trimethyl benzene | 45.20 | 169.38 |
| Hemimellitene | 12.15 | 176.08 |
The C9 aromatic raw material through separation obtain between, the yield of p-methyl-ethylbenzene calculates by following formula:
The separating technology condition of embodiment 1-6 and separating resulting are listed in table 2-4 respectively.
The separating resulting of table 4 embodiment 1-6
As can be seen from the above results: according to selected urgency agent kind difference, the inlet amount difference, the reflux ratio difference, adopt method of the present invention all can obtain purity＞98% between, the p-methyl-ethylbenzene product, its yield＞85%, separating effect is remarkable.
Comparative Examples
At first, 1000 gram C9 aromatic raw materials (component and content thereof see Table 1) are introduced from the middle part of lightness-removing column, draw the component that mainly contains n-proplbenzene, m-methyl ethylbenzene from cat head, draw the heavy constituent that mainly contain sym-trimethylbenzene, o-methylethylbenzene, unsym-trimethyl benzene and hemimellitene from tower reactor;
Then, the heavy constituent of being drawn by the lightness-removing column tower reactor are introduced weight-removing column from the middle part of weight-removing column, and between drawing from this column overhead, the p-methyl-ethylbenzene mix product, the heavy constituent that mainly contain sym-trimethylbenzene, o-methylethylbenzene, unsym-trimethyl benzene and hemimellitene are drawn from tower reactor.
Table 5 has provided the concrete operations parameter of weight-removing column and lightness-removing column, table 6 provided obtain between, the composition (weight %) of p-methyl-ethylbenzene mix product.
Use this method, by separate in the C9 aromatic obtain between, the yield of p-methyl-ethylbenzene mix product is 53.5%,, the weight content of p-methyl-ethylbenzene is 94.5%.
The operating parameters of table 5 Comparative Examples lightness-removing column and weight-removing column
| Project | Lightness-removing column | Weight-removing column |
| Stage number/piece | 140 | 80 |
| Tower top temperature ℃ | 158 | 161 |
| Tower reactor temperature ℃ | 180 | 185 |
| Tower top pressure/MPa | 0.1 | 0.1 |
| Tower reactor pressure/MPa | 0.15 | 0.13 |
| Reflux ratio | 47 | 35 |
The composition (weight %) of table 6 Comparative Examples weight-removing column and the logistics of lightness-removing column cat head tower reactor
| The logistics title | The lightness-removing column top | The lightness-removing column still | The weight-removing column top | The weight-removing column still |
| P-Xylol | 4.3 | - | - | - |
| Isopropyl benzene | 6.6 | - | - | - |
| N-proplbenzene | 59.8 | 0.04 | - | - |
| M-methyl ethylbenzene | 28.2 | 15.96 | 76.0 | 6.2 |
| P-methyl-ethylbenzene | 1.1 | 6.6 | 18.5 | 4.7 |
| Sym-trimethylbenzene | - | 7.32 | 1.4 | 8.2 |
| O-methylethylbenzene | - | 8.18 | 1.2 | 9.3 |
| Unsym-trimethyl benzene | - | 48.8 | - | 56.6 |
| Hemimellitene | - | 13.1 | - | 15.2 |
| Load (g) | 70 | 930 | 130 | 800 |
The comparison of table 7 Comparative Examples and embodiment 4 compartments, p-methyl-ethylbenzene mixture
More as can be known, the lightness-removing column reflux ratio is 47 in the rectification method, namely from the data on reflux ratio one hurdle of table 7, the flux peak of lightness-removing column is 48 ton hours, can obtain 1 ton of product, and in same tower, the product that adopts benzene with catalytic rectifying method can obtain 3.69 tons adds the urgency agent, the urgency agent of deduction 5% can obtain 3.5 tons of products, therefore, adopt method of the present invention, between obtaining, p-methyl-ethylbenzene mixture purity and yield be significantly improved, and can reach high-quality, aim of high yield.
Claims (8)
1. the method for a compartment from C9 aromatic, p-methyl-ethylbenzene mixture adopts rectifying, it is characterized in that:
Add to urge agent in rectifying, described urgency agent is a kind of in acetonitrile and the propionitrile.
As claimed in claim 1 from C9 aromatic the method for compartment, p-methyl-ethylbenzene mixture, it is characterized in that:
Described urgency agent is propionitrile.
As claimed in claim 1 or 2 from C9 aromatic the method for compartment, p-methyl-ethylbenzene mixture, it is characterized in that: comprise following steps:
(1) introduces lightness-removing column with the C9 aromatic mixture with after urging agent to mix, draw the light constituent that comprises n-proplbenzene, isopropyl benzene and urgency agent by the lightness-removing column top, drawn the heavy constituent that contain m-methyl ethylbenzene, p-methyl-ethylbenzene, sym-trimethylbenzene, o-methylethylbenzene, unsym-trimethyl benzene and hemimellitene by the lightness-removing column still
Wherein said C9 aromatic mixture is 1: 0.01～0.5 with the weight ratio of urging agent;
(2) light constituent described in the step (1) is introduced first and taken off urgency agent tower, take off by first and urge the agent cat head to draw the urgency agent, take off by first and urge the agent tower reactor to draw the light constituent logistics that contains n-proplbenzene, isopropyl benzene;
(3) introduce weight-removing column with heavy constituent described in the step (1) with after urging agent to mix, draw the logistics that comprises m-methyl ethylbenzene, p-methyl-ethylbenzene and urgency agent by the weight-removing column top, drawn the component that contains sym-trimethylbenzene, o-methylethylbenzene, unsym-trimethyl benzene and hemimellitene by the weight-removing column still
Wherein said heavy constituent are 1: 0.01～0.5 with the weight ratio of urging agent;
(4) logistics that the weight-removing column described in the step (3) top is drawn is introduced second and is taken off and urge the agent tower, take off by second and urge the agent cat head to draw the urgency agent, by second take off urge the agent tower reactor draw between, the p-methyl-ethylbenzene mixture.
As claimed in claim 3 from C9 aromatic the method for compartment, p-methyl-ethylbenzene mixture, it is characterized in that:
Described C9 aromatic mixture is 1: 0.05～0.3 with the weight ratio of urging agent;
Described heavy constituent are 1: 0.05～0.3 with the weight ratio of urging agent.
As claimed in claim 4 from C9 aromatic the method for compartment, p-methyl-ethylbenzene mixture, it is characterized in that:
Described C9 aromatic mixture is 1: 0.05～0.1 with the weight ratio of urging agent;
Described heavy constituent are 1: 0.05～0.1 with the weight ratio of urging agent.
As claimed in claim 3 from C9 aromatic the method for compartment, p-methyl-ethylbenzene mixture, it is characterized in that:
The stage number of described lightness-removing column is 30～100, and tower top temperature is 80～170 ℃, and tower top pressure is 0.1～0.5MPa, and the tower reactor temperature is 170～210 ℃, and tower reactor pressure is 0.12～0.8MPa, and reflux ratio is 5～20;
Described first stage number of taking off urgency agent tower is 5～20, and tower top temperature is 80～140 ℃, and tower top pressure is 0.1～0.5MPa, and the tower reactor temperature is 150～190 ℃, and tower reactor pressure is 0.11～0.8MPa, and reflux ratio is 2～15;
The stage number of described weight-removing column is 30～90, and tower top temperature is 80～180 ℃, and tower top pressure is 0.1～0.5MPa, and the tower reactor temperature is 170～210 ℃, and tower reactor pressure is 0.12～0.8MPa, and reflux ratio is 5～20;
Described second stage number of taking off urgency agent tower is 5～20, and tower top temperature is 80～140 ℃, and tower top pressure is 0.1～0.5MPa, and the tower reactor temperature is 150～190 ℃, and tower reactor pressure is 0.11～0.8MPa, and reflux ratio is 2～15.
As claimed in claim 6 from C9 aromatic the method for compartment, p-methyl-ethylbenzene mixture, it is characterized in that:
The stage number of described lightness-removing column is 50～70, and tower top temperature is 90～160 ℃, and tower top pressure is 0.1～0.3MPa, and the tower reactor temperature is 175～190 ℃, and tower reactor pressure is 0.12～0.4MPa, and reflux ratio is 7～14;
Described first stage number of taking off urgency agent tower is 8～15, and tower top temperature is 80～120 ℃, and tower top pressure is 0.1～0.3MPa, and the tower reactor temperature is 155～170 ℃, and tower reactor pressure is 0.11～0.4MPa, and reflux ratio is 2～5;
The stage number of described weight-removing column is 40～60, and tower top temperature is 90～160 ℃, and tower top pressure is 0.1～0.3MPa, and the tower reactor temperature is 175～190 ℃, and tower reactor pressure is 0.12～0.4MPa, and reflux ratio is 7～12;
Described second stage number of taking off urgency agent tower is 8～15, and tower top temperature is 80～120 ℃, and tower top pressure is 0.1～0.3MPa, and the tower reactor temperature is 155～170 ℃, and tower reactor pressure is 0.11～0.4MPa, and reflux ratio is 2～5.
As claimed in claim 3 from C9 aromatic the method for compartment, p-methyl-ethylbenzene mixture, it is characterized in that:
Described C9 aromatic mixture from the platinum reforming tower at the bottom of oil, xylene isomerization byproduct, in the middle of it, the content of p-methyl-ethylbenzene is 15～40 weight %.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010257340 CN102372576B (en) | 2010-08-19 | 2010-08-19 | Method for separating m-methylethylbenzene and p-methylethylbenzene mixture from C9 aromatic hydrocarbon |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010257340 CN102372576B (en) | 2010-08-19 | 2010-08-19 | Method for separating m-methylethylbenzene and p-methylethylbenzene mixture from C9 aromatic hydrocarbon |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102372576A CN102372576A (en) | 2012-03-14 |
| CN102372576B true CN102372576B (en) | 2013-08-14 |
Family
ID=45791866
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201010257340 Active CN102372576B (en) | 2010-08-19 | 2010-08-19 | Method for separating m-methylethylbenzene and p-methylethylbenzene mixture from C9 aromatic hydrocarbon |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102372576B (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4554398A (en) * | 1984-10-29 | 1985-11-19 | Exxon Research & Engineering Co. | Process for the separation of C9 aromatic isomers |
| US4996388A (en) * | 1990-07-26 | 1991-02-26 | The Dow Chemical Company | Separation of ethyltoluene isomers |
| CN1513818A (en) * | 2003-06-30 | 2004-07-21 | ����ʦ����ѧ | Rectification and extraction crossing and combining separation process of carbon 9 arene |
| CN101723790A (en) * | 2008-10-30 | 2010-06-09 | 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 |
-
2010
- 2010-08-19 CN CN 201010257340 patent/CN102372576B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4554398A (en) * | 1984-10-29 | 1985-11-19 | Exxon Research & Engineering Co. | Process for the separation of C9 aromatic isomers |
| US4996388A (en) * | 1990-07-26 | 1991-02-26 | The Dow Chemical Company | Separation of ethyltoluene isomers |
| CN1513818A (en) * | 2003-06-30 | 2004-07-21 | ����ʦ����ѧ | Rectification and extraction crossing and combining separation process of carbon 9 arene |
| CN101723790A (en) * | 2008-10-30 | 2010-06-09 | 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 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102372576A (en) | 2012-03-14 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105367368B (en) | The method that high-purity isobutylene is prepared from C_4 hydrocarbon | |
| CN101723790B (en) | Method for separating mixture of m-ethyltoluene and o-ethyltoluene from C9 aromatics | |
| CN103073383B (en) | Method and device for separating isohexane, n-hexane and benzene | |
| CN103361118A (en) | Method for recovering aromatic hydrocarbons from gasoline containing olefin and sulfide | |
| CN103121908B (en) | Method for separating mesitylene via extractive distillation | |
| CN108840789A (en) | A kind of synthesis and production method of ethylene glycol mono-tert-butyl ether | |
| CN103360195A (en) | Method for separation and purification of 1-octylene from hydrocarbon (oxygen) mixture | |
| CN102399125B (en) | Method for separating mixture of m-ethyltoluene and p-ethyltoluene from C9 aromatics | |
| CN204454944U (en) | A kind of desulfurizer of sulfur methyl tertiary butyl ether product | |
| CN105602613B (en) | The method of phenol, aromatic hydrocarbons and alkane in one-step method separation coal direct liquefaction oil | |
| CN104591952A (en) | Method for refining mesitylene by virtue of differential pressure thermal coupling rectification | |
| CN101468938B (en) | Composite solvent for extracting, distilling and separating styrene in hydrocarbons mixture, and method therefor | |
| CN102432423B (en) | Method for refining crude dimethylbenzenes by extraction and rectification | |
| CN106966852B (en) | The method of continuous extraction rectifying separation high-carbon n-alkane and normal olefine | |
| CN102372576B (en) | Method for separating m-methylethylbenzene and p-methylethylbenzene mixture from C9 aromatic hydrocarbon | |
| CN102924211B (en) | Solvent composition for separating m-methyl-ethylbenzene from p-methyl-ethylbenzene by extractive distillation and extractive distillation method | |
| CN102795957B (en) | Method for separating m-ethyltoluene and p-ethyltoluene by extractive distillation | |
| CN105503499A (en) | Separation method for extractive rectification of m/4-ethyltoluene from C9 aromatic hydrocarbon mixture | |
| CN102180760B (en) | Method for preparing benzene-free heptane solvent | |
| CN102372577B (en) | Method for concentrating sym-trimethylbenzene from C9 arenes | |
| CN101723791B (en) | Method for enriching mesitylene from C9 aromatics | |
| CN102464556B (en) | Method for separating pseudocumene from C9 aromatic hydrocarbon | |
| CN106187717B (en) | The method for being thermally integrated variable-pressure rectification separation methyl tertiary butyl ether(MTBE) and methanol azeotrope | |
| CN102924212A (en) | Solvent composition for separating mesitylene by extractive distillation and extractive distillation method | |
| CN102399124B (en) | Method for enriching mesitylene from C9 aromatics |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |