CN106608794B - The method of oxygen-containing organic compound impurity in Arene removal logistics - Google Patents
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Abstract
The present invention relates to a kind of method of oxygen-containing organic compound impurity in Arene removal logistics, mainly solve the problems, such as that a small amount of oxygen-containing organic compound contained in oxygenatedchemicals aromatic hydrocarbons reaction product in the prior art causes catalyst used in paraxylene production process and adsorbent to be poisoned.The present invention is by using following steps: 1) providing the arene stream comprising at least one of benzene,toluene,xylene, carbon nine and its above aromatic hydrocarbons, the arene stream includes the oxygen-containing organic compound of at least 10ppm mass fraction；2) make the arene stream by oxygen-containing organic compound removal unit to remove oxygen-containing organic compound impurity therein, the mass fraction of oxygen-containing organic compound impurity is less than the technical solution of 10ppm in purified arene stream, it preferably solves the above problem, can be used in the industrial production of oxygenatedchemicals aromatic hydrocarbons.
Description
Technical field
The present invention relates to a kind of methods of oxygen-containing organic compound impurity in Arene removal logistics.
Technical background
Aromatic hydrocarbons, especially benzene and paraxylene) it is important basic organic chemical industry raw material.Benzene can synthesize a series of benzene
Derivative, such as styrene, phenol, alkylbenzene；And paraxylene is numerous in chemical fibre, synthetic resin, pesticide, medicine, plastics etc.
Chemical production field has extensive purposes.Typical paraxylene production method industrial at present is using naphtha catalysis weight
Adjusting technique generates the BTX aromatics containing substances such as benzene,toluene,xylene, carbon nine and its above aromatic hydrocarbons, subsequent to pass through aromatic hydrocarbons again
Combined unit produces paraxylene.Wherein paraxylene is to separate (abbreviation adsorbing separation) by molecular sieve moving-bed adsorption
Technology or cryogenic crystallization separation separate it from boiling point therewith similar xylene different structure mixture, remaining ortho position
Pass through C with the dimethylbenzene of meta position8A isomerization (abbreviation isomerization) reaction, is allowed to be isomerized to paraxylene.Meanwhile it will reform
The toluene and carbon nine and its above aromatic hydrocarbons that unit generates pass through toluene and carbon nine and its above aromatic disproportion and transalkylation (abbreviation
Toluene disproportionation) react generation benzene and C8A, to increase production C8A, and then produce paraxylene.
In recent years, since oil supply day is becoming tight, crude oil price remains high for a long time, and also water rises the production cost of aromatic hydrocarbons
Height.In conjunction with the higher and higher national conditions of rich coal resources in China and petroleum interdependency, develop the coal with cost of material advantage
Aromatic hydrocarbons technology processed becomes the research hotspot of last decade.By lasting research, it is prominent which achieves biggish technology in recent years
Broken, coal-based methanol aromatic hydrocarbons technology has been completed that Industrial demonstration is tested.
The raw material of aromatics production has been widened relative to conventional petroleum route through methanol or dimethyl ether aromatic hydrocarbons technology using coal
Source, and there is certain cost advantage.But methanol inevitably generates a variety of contain during aromatization
The non-aromatic oxygenatedchemicals such as oxygen organic compound, including acetaldehyde, acetone further includes a series of aromatic series oxygenatedchemicals, such as benzene
Phenol, methylphenol, xylenol, benzaldehyde, benzyl carbinol etc..If these oxygenatedchemicals enter subsequent virtue with aromatic hydrocarbons material
Hydrocarbon separation and aromatic hydrocarbons conversion reaction unit (such as toluene disproportionation, isomerization, paraxylene adsorbing separation), it will cause in catalyst
Poison or the decline of adsorbent absorption property, seriously affect the normal production of paraxylene, therefore, these oxygenatedchemicals must be subject to
Removing.
A kind of aromatic hydrocarbons methanol alkylation method for removing oxygenatedchemicals impurity is disclosed in CN103664488 patent.It should
Method, which passes through, forms the reaction raw materials containing methanol, benzene, toluene in methylation catalyst and oxygenatedchemicals Removal of catalyst
Composite catalyst on simultaneously methylation reaction and oxygenatedchemicals elimination reaction occurs, reaction product obtains after water-oil separating
Boiling point must be contained only in the aromatic naphtha phase of benzene oxygenatedchemicals below.Then the aromatic naphtha mutually in stripper removed overhead these
Boiling point obtains the aromatic hydrocarbons that oxygenatedchemicals mass content is lower than 0.5ppm in benzene oxygenatedchemicals below, tower reactor.This method is only
The removing for considering non-aromatic oxygenatedchemicals, without considering the removing of aromatic series oxygenatedchemicals and its to subsequent reactions unit
The influence of catalyst.And the boiling point of these aromatic series oxygenatedchemicals is much higher than benzene, can not remove in stripper.In addition methyl
Change reaction and generate a large amount of water, keeps the partial pressure of oxygenatedchemicals in methylation reaction product lower, composite catalyst is unable to reach
Optimal oxygenate conversion effect.
A kind of method for removing oxygenatedchemicals in hydrocarbon material flow is disclosed in CN103418164 patent.This method will contain
Have the hydrocarbon material flow of oxygenatedchemicals temperature be 0~85 DEG C, pressure is 0.1~40bar and air speed is 200~10000/
The oxygenatedchemicals removed in hydrocarbon material flow is contacted under conditions of hr with solid absorbent, contains oxidation in purified hydrocarbon material flow
The mass concentration for closing object is not more than 1ppm.But this method is mainly for methanol, dimethyl ether or water in C2~C5 hydro carbons of gas phase
The removing of equal oxygenatedchemicals, does not account for the removing of aromatic hydrocarbons race oxygenatedchemicals in the arene stream of liquid phase.
A kind of method that oxygenatedchemicals is removed from olefin stream is disclosed in CN101993321 patent.This method is logical
It crosses and removes oxygenatedchemicals from olefin stream by the way of being segmented variable-pressure rectification.The tower first in first oxide removal tower
Kettle removes water, and tower reactor removes oxygenatedchemicals in second oxide removal tower, and tower top obtains in third oxide removal tower
Purified olefin stream, tower reactor obtain the logistics containing oxygenatedchemicals and return to second oxide removal tower.This method has
It does not need addition absorbent, ethylene, propylene and loses few advantage, but complicated for operation and energy consumption is high, equipment investment is big.
CN103772097 patent discloses a kind of alkylate processing method.Alkylation reaction product feeding is filled with
The adsorbent bed of solid base adsorbent, the reaction product after obtaining depickling.CN103772096 patent discloses another removing alkyl
Change the method for organic acid in product.Alkylate first passes through the cooling of reaction product cooling system, enters back into level-one water-oil separating
Device, isolates primary oil phase and level-one water phase, and primary oil divides in second level oil water separator after mutually mixing in water washing tank with water
From oily phase after being purified.The method of above-mentioned two patent disclosure is taken off for the organic acid in alkylation aromatic products
It removes, also without the removing for considering aromatic hydrocarbons race oxygenatedchemicals.
The prior art does not carry out targetedly aromatic hydrocarbons oxygenatedchemicals in oxygenatedchemicals aromatic hydrocarbons reaction product
Removing, there are aromatic hydrocarbons oxygenatedchemicals cause alkylation catalyst in subsequent cell, disproportionation catalyst, isomerization catalyst and
Adsorbent poisoning, catalyst life short the problem of needing frequent regeneration, the present invention targetedly solves the above problem.
Summary of the invention
It is fragrant in oxygenatedchemicals aromatic hydrocarbons reaction product the technical problem to be solved by the present invention is to exist in the prior art
It is short that hydro carbons oxygen-containing organic compound easily leads to alkylation catalyst, toluene disproportionation catalyst, isomerization catalyst poisoning and service life
And the problems such as paraxylene adsorbing separation sorbent used adsorption capacity decline, it provides in a kind of new Arene removal logistics
The method of oxygen-containing organic compound impurity.This method, which has, extends alkylation catalyst, toluene disproportionation catalyst, isomerization catalytic
Agent service life and the advantages of keep paraxylene adsorbing separation sorbent used adsorption activity.
To solve the above problems, The technical solution adopted by the invention is as follows: a kind of oxygen-containing organic in Arene removal logistics
The method for closing object impurity, method includes the following steps: 1) providing comprising in benzene,toluene,xylene, carbon nine and its above aromatic hydrocarbons
At least one arene stream, the arene stream include the oxygen-containing organic compound of at least 10ppm mass fraction；2) make described
Arene stream is by oxygen-containing organic compound removal unit to remove oxygen-containing organic compound impurity therein, purified aromatic hydrocarbons
The mass fraction of oxygen-containing organic compound impurity is less than 10ppm in logistics.
In above-mentioned technical proposal, it is preferable that the arene stream is obtained by methanol and/or dimethyl ether through aromatization.
In above-mentioned technical proposal, it is preferable that benzene,toluene,xylene in the arene stream, carbon nine and its above aromatic hydrocarbons
Gross mass content is greater than 60%.
In above-mentioned technical proposal, it is preferable that the oxygen-containing organic compound include propionic aldehyde, acetone, methanol, acetic acid, phenols,
One of aromatic alcohol, aromatic aldehyde are a variety of.
In above-mentioned technical proposal, it is preferable that the quality of oxygen-containing organic compound impurity in the purified arene stream
Score is less than 5ppm；It is furthermore preferred that the mass fraction of oxygen-containing organic compound impurity is less than in the purified arene stream
1ppm。
In above-mentioned technical proposal, the mass fraction of oxygen-containing organic compound is at least 50ppm in the arene stream.It is preferred that
, the mass fraction of oxygen-containing organic compound is at least 100ppm in the arene stream.It is furthermore preferred that in the arene stream
The mass fraction of oxygen-containing organic compound is at least 1000ppm.
In above-mentioned technical proposal, it is preferable that the oxygen-containing organic compound removal unit is using absorption, washing, distillation, extraction
It one of the methods of takes, react or any form of combination of a variety of methods.Preferably, have using the method removing of absorption is oxygen-containing
Machine compound.Preferably, oxygen-containing organic compound is removed using the combined method of reaction and absorption.Preferably, using washing and
The combined method of absorption removes oxygen-containing organic compound.Preferably, oxygen-containing organic using the removing of the combined method of distillation and absorption
Compound.
In above-mentioned technical proposal, it is preferable that purified arene stream through in alkylation, toluene disproportionation or isomerization extremely
A kind of few reaction；It is highly preferred that purified arene stream is handled through alkylation；It is highly preferred that purified arene stream warp
Toluene disproportionation processing；It is highly preferred that purified arene stream is handled through isomerization.
Oxygen-containing organic compound generates the reaction containing aromatic hydrocarbons, light hydrocarbons and water through aromatization and produces in the present invention
Object, the reaction product obtain arene stream by three phase separation.Contain the main mesh such as benzene,toluene,xylene in the arene stream
Product is marked, simultaneously containing non-aromaticss oxygenatedchemicals and phenol, methylphenol, xylenol, benzyl carbinol, benzene such as aldehyde, ketone, acid
The aromatic series oxygenatedchemicals such as acetaldehyde.Oxygenatedchemicals boiling point distribution involved in the present invention is extensive, and takes off in the prior art
Except the method for oxygenatedchemicals does not recognize high boiling aromatic series oxygenatedchemicals to later separation unit and reaction member
The significant negative impact of middle catalyst and adsorbent, it is bad to removal effect of the aromatic series oxygenatedchemicals in aromatic hydrocarbons.Using
Method of the invention can be such that the oxygenatedchemicals mass content in arene stream controls in 10ppm hereinafter, avoiding subsequent cell
Middle alkylation catalyst, toluene disproportionation catalyst, isomerization catalyst poisoning, extend catalyst life, avoid adsorbing separation list
The decline of adsorbent adsorption capacity used in member, guarantees the smooth long term running and aromatic hydrocarbon product quality of device, achieves preferably
Effect.
Detailed description of the invention
Fig. 1 is one of the flow diagram of the method for the invention.
Fig. 2 is the two of the flow diagram of the method for the invention.
Fig. 3 is the three of the flow diagram of the method for the invention.
In Fig. 1,11 be aromatic feed；12 be carbon seven and more light component；13 be de- oxygenatedchemicals carbon seven and lighter group
Point；14 be carbon eight and more heavy constituent；15 be the carbon eight and more light component of de- oxygenatedchemicals；101 be toluene knockout tower；102 are
Non-aromatic oxygenatedchemicals adsorbent bed；103 be aromatic series oxygenatedchemicals adsorbent bed.
Fig. 1 process description is as follows: aromatic feed 11 is sent into toluene knockout tower 101, is separated into carbon seven and more 12 He of light component
Carbon eight and more heavy constituent 14.Carbon seven and more light component 12 are sent into non-aromatic oxygenatedchemicals adsorbent bed 102, and acquisition takes off oxygen-containing chemical combination
The carbon seven of object and more light component 13.Carbon eight and more heavy constituent 14 are sent into aromatic series oxygenatedchemicals adsorbent bed 103, and the de- of acquisition contains
The carbon eight of oxygen compound and more heavy constituent 15.In Fig. 2,21 be aromatic feed；22 be light dydrocarbon and more light component；23 contain oxidation to be de-
Close the light dydrocarbon and more light component of object；24 be carbon six and more heavy constituent；25 be the carbon six and more light component of de- oxygenatedchemicals；26 are
Hydrogen；201 be depentanizer；202 be non-aromatic oxygenatedchemicals adsorbent bed；203 be hydrogenation deoxidation reactor.
Fig. 2 process description is as follows: aromatic feed 21 is sent into depentanizer 201, is separated into light dydrocarbon and more light component 22 and carbon
Six and more heavy constituent 24.Light dydrocarbon and more light component 22 are sent into non-aromatic oxygenatedchemicals adsorbent bed 202, remove non-aromatic oxygen-containing chemical combination
Object.Carbon six and more heavy constituent 24 and hydrogen 26 are sent into hydrogenation deoxidation reactor 203, generate the carbon six of de- oxygenatedchemicals and lighter
Component.
In Fig. 3,31 be aromatic feed；32 be carbon seven and more light component；33 be water；34 be waste water；35 is oxygen-containing once to take off
Compound light oil；36 be secondary de- oxygenatedchemicals light oil；37 be carbon eight and more heavy constituent；38 be de- oxygenatedchemicals aromatic hydrocarbons；
301 be toluene knockout tower；302 mutually wash unit for oil；303 be non-aromatic oxygenatedchemicals adsorbent bed；304 be aromatic series containing oxidation
Close object adsorbent bed.
Fig. 3 process description is as follows: aromatic feed 31 is sent into toluene knockout tower 301, is separated into carbon seven and more 32 He of light component
Carbon eight and more heavy constituent 37.Carbon seven and more light component 32 are sent into Gravity Separation after oily mutually washing unit 302 and the mixing of water 33, obtain
Once de- oxygenatedchemicals light oil 35 and waste water 34.Then once de- oxygenatedchemicals light oil 35 is sent into non-aromatic oxygenatedchemicals suction
Attached bed 303 removes non-aromatic oxygenatedchemicals, the carbon seven of the de- oxygenatedchemicals of acquisition and more light component 36.Carbon eight and more heavy constituent
37, which are sent into aromatic series oxygenatedchemicals adsorbent bed 304, removes aromatic series oxygenatedchemicals, the carbon eight of the de- oxygenatedchemicals of acquisition
And more heavy constituent 38.
The present invention will be further described below by way of examples, but is not limited only to the present embodiment.
Specific embodiment
[embodiment 1]
Reaction product from aromatization of methanol reactor passes through three phase separation, obtains gas phase lighter hydrocarbons, water phase and oily phase,
Middle oil is mutually as the aromatic feed 11 of de- oxygenatedchemicals.The mass flow of aromatic feed 11 is 3 ton/hours, includes 2.5wt%
Benzene, 13.4wt% toluene, 54.1wt% dimethylbenzene, 0.5wt% methanol, the non-aromatic oxygenatedchemicals of 0.26wt%, 0.11wt% virtue
Fragrant race's oxygenatedchemicals.Toluene knockout tower 101 is sent into the charging after pump is pressurized to 0.4MPa, is separated into carbon seven and lighter group
Points 12 and carbon eight and more heavy constituent 14.The number of plates of toluene knockout tower 101 is 45, reflux ratio 1.6, and tower top operating pressure is
0.3MPa, operation temperature are 45 DEG C, and bottom temperature is 214 DEG C.The mass flow of carbon seven and more light component 12 be 0.75 ton/it is small
When, include 10wt% benzene, 53.6wt% toluene, 2wt% methanol, the non-aromatic oxygenatedchemicals of 1.04wt%, without aromatic series it is oxygen-containing
Compound.The mass flow of carbon eight and more heavy constituent 14 is 2.25 ton/hours, including 72.13wt% dimethylbenzene, 0.15wt% virtue
Fragrant race's oxygenatedchemicals.Carbon seven and more light component 12 are sent into non-aromatic oxygenatedchemicals adsorbent bed 102, remove non-aromatic oxygen-containing chemical combination
Object, wherein non-aromatic oxygenatedchemicals adsorbent bed 102 uses 5A type adsorbent of molecular sieve, adsorption temp is 50 degrees Celsius, adsorption pressure
Power is 2.1MPa, and the carbon seven of the de- oxygenatedchemicals of acquisition and more 13 oxygenatedchemicals mass content of light component are 9ppm.Carbon eight
And more heavy constituent 14 is sent into aromatic series oxygenatedchemicals adsorbent bed 103, removes aromatic series oxygenatedchemicals, wherein aromatic series is oxygen-containing
Compound adsorbent bed 103 uses 13X type adsorbent of molecular sieve, and adsorption temp is 45 degrees Celsius, adsorptive pressure 1.2MPa, obtains
De- oxygenatedchemicals carbon eight and more 15 oxygenatedchemicals mass content of heavy constituent be 8ppm.
[embodiment 2]
Reaction product from aromatization of methanol reactor passes through three phase separation, obtains gas phase lighter hydrocarbons, water phase and oily phase,
Middle oil is mutually as the aromatic feed 21 of de- oxygenatedchemicals.The mass flow of aromatic feed 21 is 3 ton/hours, includes 3wt%
Benzene, 13.2wt% toluene, 63.5wt% dimethylbenzene, 0.1wt% methanol, the non-aromatic oxygenatedchemicals of 0.15wt%, 0.15wt% virtue
Fragrant race's oxygenatedchemicals.Depentanizer 201 is sent into the charging after pump is pressurized to 0.3MPa, is separated into light dydrocarbon and more light component
22 and carbon six and more heavy constituent 24.The number of plates of depentanizer 201 is 40, reflux ratio 4, and tower top operating pressure is 0.26MPa,
Operation temperature is 40 DEG C, and bottom temperature is 195 DEG C.The mass flow of light dydrocarbon and more light component 22 is 0.15 ton/hour, includes
2.0wt% methanol, the non-aromatic oxygenatedchemicals of 3wt% are free of aromatic series oxygenatedchemicals.The quality stream of carbon six and more heavy constituent 24
Amount is 2.85 ton/hours, including 3.16wt% benzene, 13.9wt% toluene, 66.8wt% dimethylbenzene, 0.16wt% aromatic series are oxygen-containing
Compound.Light dydrocarbon and more light component 22 are sent into non-aromatic oxygenatedchemicals adsorbent bed 202, remove non-aromatic oxygenatedchemicals, wherein non-
Fragrant oxygenatedchemicals adsorbent bed 202 uses 5A type adsorbent of molecular sieve, and adsorption temp is 45 degrees Celsius, adsorptive pressure 2MPa,
The light dydrocarbon and more 23 oxygenatedchemicals mass content of light component of the de- oxygenatedchemicals obtained are 50ppm.Carbon six and more heavy constituent
24 are sent into hydrogenation deoxidation reactor 203, make aromatic series oxygenatedchemicals that deoxygenation occur under the action of hydrogenation catalyst, raw
At hydro carbons and water.Wherein hydrogenation catalyst is the silica-alumina supports molecular sieve catalyst containing Mo, Ni, Co, W, and reaction temperature is taken the photograph for 300
Family name's degree, reaction pressure 1.8MPa, the carbon eight of the de- oxygenatedchemicals of acquisition and more 25 oxygenatedchemicals mass content of heavy constituent
For 1ppm.
[embodiment 3]
Reaction product from aromatization of methanol reactor passes through three phase separation, obtains gas phase lighter hydrocarbons, water phase and oily phase,
Middle oil is mutually as the aromatic feed 31 of de- oxygenatedchemicals.The mass flow of aromatic feed 31 is 10 ton/hours, includes
1.3wt% benzene, 15.5wt% toluene, 72.1wt% dimethylbenzene, 0.7wt% methanol, the non-aromatic oxygenatedchemicals of 0.4wt%,
0.09wt% aromatic series oxygenatedchemicals.Toluene knockout tower 301 is sent into the charging after pump is pressurized to 0.45MPa, is separated into
Carbon seven and more light component 32 and carbon eight and more heavy constituent 37.The number of plates of toluene knockout tower 301 is 55, reflux ratio 1.3, tower top
Operating pressure is 0.3MPa, and operation temperature is 40 DEG C, and bottom temperature is 208 DEG C.The mass flow of carbon seven and more light component 32 is
2.31 ton/hours, include 5.63wt% benzene, 67.1wt% toluene, 3wt% methanol, the non-aromatic oxygenatedchemicals of 1.73wt% is free of
Aromatic series oxygenatedchemicals.The mass flow of carbon eight and more heavy constituent 37 is 7.69 ton/hours, including 93.76wt% dimethylbenzene,
0.12wt% aromatic series oxygenatedchemicals.Carbon seven and more light component 32 are sent into oily mutually washing unit 302 and flow is 1 ton/hour
Water 33 mix after Gravity Separation, the residence time is 30 minutes, obtains once de- oxygenatedchemicals light oil 35 and waste water 34.Its
In, wastewater quality flow is 1.09 ton/hours, 5.89wt% containing methanol；Once de- 35 mass flow of oxygenatedchemicals light oil is
2.22 ton/hours, 0.27wt% containing methanol.Then once de- oxygenatedchemicals light oil 35 is sent into non-aromatic oxygenatedchemicals adsorbent bed
The 303 non-aromatic oxygenatedchemicals of removing, wherein non-aromatic oxygenatedchemicals adsorbent bed 303 uses 5A type adsorbent of molecular sieve, absorption temperature
Degree is 40 degrees Celsius, adsorptive pressure 1.5MPa, the carbon seven of the de- oxygenatedchemicals of acquisition and more 36 oxygenatedchemicals of light component
Mass content is 3ppm.Carbon eight and more heavy constituent 37 are sent into aromatic series oxygenatedchemicals adsorbent bed 304 and remove aromatic series containing oxidation
Object is closed, wherein aromatic series oxygenatedchemicals adsorbent bed 304 uses 13X type adsorbent of molecular sieve, and adsorption temp is 40 degrees Celsius, inhales
Enclosure pressure is 1.5MPa, and the carbon eight of the de- oxygenatedchemicals of acquisition and more 38 oxygenatedchemicals mass content of heavy constituent are 6ppm.
[embodiment 4]
Reaction product from aromatization of methanol reactor passes through three phase separation, obtains gas phase lighter hydrocarbons, water phase and oily phase,
Middle oil is mutually as the aromatic feed 31 for taking off oxygenatedchemicals.The mass flow of aromatic feed 31 is 10 ton/hours, includes
0.3wt% benzene, 18wt% toluene, 72wt% dimethylbenzene, the non-aromatic oxygenatedchemicals of 0.005wt%, 0.0018wt% aromatic series contain
Oxygen compound.Toluene knockout tower 301 is sent into the charging after pump is pressurized to 0.45MPa, is separated into carbon seven and more light component 32
With carbon eight and more heavy constituent 37.The number of plates of toluene knockout tower 301 is 60, reflux ratio 1.2, and tower top operating pressure is
0.3MPa, operation temperature are 40 DEG C, and bottom temperature is 211 DEG C.The mass flow of carbon seven and more light component 32 is 2.5 ton/hours,
Comprising the non-aromatic oxygenatedchemicals of 0.02wt%, aromatic series oxygenatedchemicals is free of.The mass flow of carbon eight and more heavy constituent 37 is
7.5 ton/hours, including 0.0054wt% aromatic series oxygenatedchemicals.Carbon seven and more light component 32 are sent into oily mutually washing unit 302
Gravity Separation after the water 33 for being 1 ton/hour with flow mixes, residence time are 30 minutes, and it is light to obtain once de- oxygenatedchemicals
Oil 35 and waste water 34.Then once de- oxygenatedchemicals light oil 35 is sent into non-aromatic oxygenatedchemicals adsorbent bed 303 and removes non-aromatic contain
Oxygen compound, wherein non-aromatic oxygenatedchemicals adsorbent bed 303 uses 5A type adsorbent of molecular sieve, adsorption temp is 40 degrees Celsius,
Adsorptive pressure is 1.5MPa, and the carbon seven of the de- oxygenatedchemicals of acquisition and more 36 oxygenatedchemicals mass content of light component are
1ppm.Carbon eight and more heavy constituent 37 are sent into aromatic series oxygenatedchemicals adsorbent bed 304 and remove aromatic series oxygenatedchemicals, wherein virtue
Fragrant race's oxygenatedchemicals adsorbent bed 304 uses 13X type adsorbent of molecular sieve, and adsorption temp is 40 degrees Celsius, and adsorptive pressure is
1.5MPa, the carbon eight of the de- oxygenatedchemicals of acquisition and more 38 oxygenatedchemicals mass content of heavy constituent are 2ppm.
[comparative example 1]
By process flow shown in embodiment 4.Aromatic feed 31 includes the non-aromatic oxygenatedchemicals of 0.005wt%,
0.0018wt% aromatic series oxygenatedchemicals.Toluene knockout tower 301 is sent into the charging after pump is pressurized to 0.45MPa, separation
For carbon seven and more light component 32 and carbon eight and more heavy constituent 37.Carbon seven and more light component 32 does not remove oxygenatedchemicals, directly send
Enter benzene column, toluene tower, isolates benzene and toluene.Toluene is sent into toluene disproportionation and transalkylation.Due to containing in toluene
Oxygen compound leads to the toluene disproportionation catalyst lost of life 3%.Carbon eight and more heavy constituent 37 does not remove oxygenatedchemicals, through two
Toluene tower is sent directly into xylene isomerization unit after isolating dimethylbenzene, and isomerization catalyst performance is caused to decline, regeneration week
Phase shortens 5%.
Claims (9)
1. a kind of method of oxygen-containing organic compound impurity in Arene removal logistics, method includes the following steps: 1) provide by
The arene stream that methanol and/or dimethyl ether are obtained through aromatization, the arene stream include benzene,toluene,xylene, carbon nine
And its at least one of above aromatic hydrocarbons, the arene stream include the oxygen-containing organic compound of at least 10ppm mass fraction；2) make
The arene stream by oxygen-containing organic compound removal unit to remove oxygen-containing organic compound impurity therein, it is purified
The mass fraction of oxygen-containing organic compound impurity is less than 10ppm in arene stream；Wherein, the oxygen-containing organic compound includes virtue
Hydro carbons oxygen-containing organic compound.
2. according to claim 1 in Arene removal logistics oxygen-containing organic compound impurity method, it is characterised in that it is described
The gross mass content of benzene,toluene,xylene, carbon nine and its above aromatic hydrocarbons is greater than 60% in arene stream.
3. according to claim 1 in Arene removal logistics oxygen-containing organic compound impurity method, it is characterised in that it is described
Oxygen-containing organic compound includes at least one of propionic aldehyde, acetone, methanol, acetic acid, phenols, aromatic alcohol and aromatic aldehyde.
4. according to claim 1 in Arene removal logistics oxygen-containing organic compound impurity method, it is characterised in that it is described
The mass fraction of oxygen-containing organic compound impurity is less than 5ppm in purified arene stream.
5. according to claim 4 in Arene removal logistics oxygen-containing organic compound impurity method, it is characterised in that it is described
The mass fraction of oxygen-containing organic compound impurity is less than 1ppm in purified arene stream.
6. according to claim 1 in Arene removal logistics oxygen-containing organic compound impurity method, it is characterised in that it is described
The mass fraction of oxygen-containing organic compound is at least 50ppm in arene stream.
7. according to claim 6 in Arene removal logistics oxygen-containing organic compound impurity method, it is characterised in that it is described
The mass fraction of oxygen-containing organic compound is at least 100ppm in arene stream.
8. according to claim 1 in Arene removal logistics oxygen-containing organic compound impurity method, it is characterised in that it is described
One of absorption, washing, distillation, extraction, reaction method can be used in oxygen-containing organic compound removal unit or a variety of methods are appointed
The combination of meaning form.
9. according to claim 1 in Arene removal logistics oxygen-containing organic compound impurity method, it is characterised in that purification
Arene stream afterwards is reacted through at least one of alkylation, toluene disproportionation or isomerization.
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| CN103418164A (en) * | 2012-05-16 | 2013-12-04 | 中国石油化工股份有限公司 | Method for removing oxygen-containing compound in hydrocarbon stream |
| CN103664488A (en) * | 2012-09-05 | 2014-03-26 | 中国石油化工股份有限公司 | Arene methanol alkylation method for removing oxygen-containing compound impurities |
| CN103664492A (en) * | 2012-09-05 | 2014-03-26 | 中国石油化工股份有限公司 | Alkylation method for methylbenzene and methyl alcohol |
| CN103864565A (en) * | 2014-03-20 | 2014-06-18 | 华电煤业集团有限公司 | System and method of preparing paraxylene by alcohol/ether conversion |
| CN107973687A (en) * | 2016-10-21 | 2018-05-01 | 中国石油化工股份有限公司 | The method of oxygenatedchemicals in methanol removal aromatization products BTX aromatics |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103418164A (en) * | 2012-05-16 | 2013-12-04 | 中国石油化工股份有限公司 | Method for removing oxygen-containing compound in hydrocarbon stream |
| CN103664488A (en) * | 2012-09-05 | 2014-03-26 | 中国石油化工股份有限公司 | Arene methanol alkylation method for removing oxygen-containing compound impurities |
| CN103664492A (en) * | 2012-09-05 | 2014-03-26 | 中国石油化工股份有限公司 | Alkylation method for methylbenzene and methyl alcohol |
| CN103864565A (en) * | 2014-03-20 | 2014-06-18 | 华电煤业集团有限公司 | System and method of preparing paraxylene by alcohol/ether conversion |
| CN107973687A (en) * | 2016-10-21 | 2018-05-01 | 中国石油化工股份有限公司 | The method of oxygenatedchemicals in methanol removal aromatization products BTX aromatics |
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