CN107286989A - A kind of method that the high-knock rating gasoline rich in BTX is produced by heavy aromatics - Google Patents

A kind of method that the high-knock rating gasoline rich in BTX is produced by heavy aromatics Download PDF

Info

Publication number
CN107286989A
CN107286989A CN201710461288.6A CN201710461288A CN107286989A CN 107286989 A CN107286989 A CN 107286989A CN 201710461288 A CN201710461288 A CN 201710461288A CN 107286989 A CN107286989 A CN 107286989A
Authority
CN
China
Prior art keywords
aromatics
heavy aromatics
heavy
btx
reaction
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.)
Pending
Application number
CN201710461288.6A
Other languages
Chinese (zh)
Inventor
臧甲忠
李健
范景新
于海斌
宫毓鹏
舒畅
赵训志
刘洋
张健
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
China National Offshore Oil Corp CNOOC
CNOOC Energy Technology and Services Ltd
CNOOC Tianjin Chemical Research and Design Institute Co Ltd
Original Assignee
China National Offshore Oil Corp CNOOC
CNOOC Energy Technology and Services Ltd
CNOOC Tianjin Chemical Research and Design Institute Co Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by China National Offshore Oil Corp CNOOC, CNOOC Energy Technology and Services Ltd, CNOOC Tianjin Chemical Research and Design Institute Co Ltd filed Critical China National Offshore Oil Corp CNOOC
Priority to CN201710461288.6A priority Critical patent/CN107286989A/en
Publication of CN107286989A publication Critical patent/CN107286989A/en
Pending legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/305—Octane number, e.g. motor octane number [MON], research octane number [RON]
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02—Gasoline

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The invention discloses a kind of method that the high-knock rating gasoline rich in BTX is produced by heavy aromatics, heavy aromatics raw material is cut into monocyclic heavy aromatics and condensed-nuclei aromatics by this method；Wherein condensed-nuclei aromatics selective hydrogenation saturation is the ring-opening reaction that naphthenic ring occurs simultaneously for monocyclic heavy aromatics, is then hydrocracked and transalkylation reaction with the monocyclic heavy aromatics mixing, high-knock rating gasoline of the generation rich in BTX.The present invention can improve condensed-nuclei aromatics conversion ratio in heavy aromatics raw material, and liquid yield is can guarantee that again, reduce dry gas, liquefied gas yield, reduction hydrogen consumption and aromatic hydrocarbons loss, reach the purpose of high-knock rating gasoline of the production rich in BTX.

Description

A kind of method that the high-knock rating gasoline rich in BTX is produced by heavy aromatics
Technical field
The present invention relates to heavy aromatics field of comprehensive utilization, and in particular to a kind of to produce the higher octane rich in BTX by heavy aromatics It is worth the method for gasoline.
Background technology
The carbon that heavy aromatics refers to the chemical process by-product such as the oil refining process such as catalytic reforming, disproportionation, isomerization and cracking of ethylene is former The aromatic hydrocarbons of subnumber nine and the above.Because crude oil in poor quality and degree of heaviness are constantly deepened, heavy oil product lighting produces lightweight Oil product is trend of the times.Heavy aromatics is a kind of valuable petrochemical industry resource, but its number of components is more, and isomer is more, separation Difficulty is big；And heavy aromatics easy coking in process, difficulty of processing is very big.
The toluene disproportionation and transalkylation technology of existing more maturation is mainly processing C9Heavy aromatics based on aromatic hydrocarbons.C9 Heavy aromatics above with primary fuel or is blended in sale in diesel oil more, has not only polluted environment but also waste of resource.Therefore, major researchs Mechanism, which is devoted to exploitation, can handle C9The hydrogenation lighting technique of above heavy aromatics.
RIPP heavy aromatics one-step method hydrogenation lighting technology, 360~460 DEG C of reaction temperature, reaction pressure 1~ 3MPa, 1~3h of weight (hourly) space velocity (WHSV)-1, hydrogen to oil volume ratio 500~1500：1, heavy aromatics is converted into the light aromatics such as BTX.But, liquid Only 85% or so is received, alkyl loss is larger, ethyl, propyl group fracture have been hydrogenated to ethane and propane.The technics comparing is fatal Defect be raw material with C9And C10Based on, C11And above feed stock conversion is relatively low.To find out its cause, to ensure that it is not excessive full that liquid is received And aromatic ring, the reaction pressure used is relatively low, and on this condition, condensed-nuclei aromatics open loop is more difficult, therefore reaction conversion ratio It is relatively low, and toluene is compared with heavy aromatics disproportionation and transalkylation technology, without competitive advantage.
Due to a step lighting be difficult take into account catalyst stability and light aromatics selectivity, two step lighting methods meet the tendency of and It is raw.Heavy aromatics is carried out monocyclic heavy aromatics and lightweight by the B of CN 104447159 by transalkylation reactor under conditions of non-hydrogen The transalkylation reaction of aromatic hydrocarbons, realizes monocyclic heavy aromatics lighting and avoids mononuclear aromatics from being hydrogenated with saturation, alkyl turns to greatest extent The cut for moving product mid-boiling point >=178 DEG C enters hydrogenation reactor progress hydrogenation lighting, and final realize improves heavy aromatics conversion While rate and liquid receipts, voluminous high added value Mixed XYLENE and C9The purpose of aromatic fraction.The shortcoming of this method is to need additionally Benzene, the toluene of addition, generate BTX unfavorable to second step lighting, it is also possible to the hydrogenation saturation loss in lighting reaction；More Fatal, heavy aromatics is under first step conditions of non-hydrogen, easily coking, heavy aromatics boiling range is become weight on the contrary, it more difficult to handle.
Heavy aromatics is carried out condensed-nuclei aromatics selective hydrogenation in selective hydrogenation reactor first and opened by the B of CN 104357084 Ring reacts, and condensed-nuclei aromatics is become the mononuclear aromatics with alkyl side chain, and product enters lighting reactor, entered in a hydrogen atmosphere The transalkylation reaction and non-aromatic cracking and aromatization of the monocyclic heavy aromatics of row and light aromatics, it is final to realize Gao Chong simultaneously Aromatics conversion rate and high aromatic hydrocarbons purity and voluminous high added value Mixed XYLENE and C9The purpose of aromatic fraction.CN 104357083 B it is also proposed the thinking of similar double diffusion.Because also containing substantial amounts of monocyclic heavy aromatics, above-mentioned two sections in heavy aromatics raw material The problem of lightening method still has aromatic hydrocarbons supersaturation, the condensed-nuclei aromatics selective hydrogenation pressure of the first step is higher or air speed It is relatively low, monocyclic heavy aromatics supersaturation is easily caused for cycloalkane, and then open loop cracking, result is that liquid receipts are low, and aromatic hydrocarbons loss is big, Produce the more intractable dry gas of low value, liquefied gas；But if first step condensed-nuclei aromatics selective hydrogenation pressure it is relatively low or Air speed is larger, and condensed-nuclei aromatics selective hydrogenation degree is inadequate, it is impossible to open loop cracking and transalkylation, does not reach the mesh of lighting , while can also influence the life-span of two-stage catalytic agent.
In summary, an either step lighting method or two sections of lighting methods, heavy aromatics raw material directly enter reactor, To ensure catalyst stabilization operation, lighting reaction is carried out under high pressure and low-speed, and this is opened after resulting in aromatic hydrocarbons supersaturation Ring crack, generates the dry gas and liquefied gas of a large amount of low values.For monocyclic heavy aromatics and condensed-nuclei aromatics, its suitable treatment conditions Clearly it is very different, laying particular stress on high liquid receipts and light aromatics can selectively cause catalyst unstable, condensed-nuclei aromatics conversion Rate is low.
The content of the invention
The technical problems to be solved by the invention be overcome prior art it is above-mentioned it is not enough there is provided a kind of loss of aromatic hydrocarbons it is small, Liquid receives the high-octane rating vapour that BTX is rich in by heavy aromatics production that high, light aromatics selectively good and catalyst can be steadily in the long term The method of oil.
The method that the present invention is produced the high-knock rating gasoline rich in BTX by heavy aromatics, this method includes：
(1) heavy aromatics is cut into light component based on monocyclic heavy aromatics and rich in condensed-nuclei aromatics with 218 DEG C first Heavy constituent；
(2) heavy constituent enters selective hydrogenation reactor progress selective hydrogenation saturation and ring-opening reaction, is changed into monocyclic heavy Aromatic hydrocarbons；
The light component that the product of (3) (2) steps is obtained with (1) step is mixed into lighting reactor and is hydrocracked And transalkylation reaction, gasoline fraction of the generation rich in BTX lightweight mononuclear aromatics, by-product dry gas, liquefied gas；
Wherein described heavy aromatics refer to carbon number be more than or equal to nine single multi- PAH, monocyclic heavy aromatics refer to containing only There is the heavy aromatics of a phenyl ring, condensed-nuclei aromatics refers to the heavy aromatics containing two and above phenyl ring.
According to the method described in the present invention, the reaction condition of preferably selecting property hydrogenation saturation and ring-opening reaction is：Reaction temperature 350~400 DEG C of degree, 3~6MPa of reaction pressure, 0.5~1.5h of weight (hourly) space velocity (WHSV)-1, hydrogen hydrocarbon volume ratio 500~1000；
It is hydrocracked the reaction condition with transalkylation reaction：380~430 DEG C of reaction temperature, 2~4MPa of reaction pressure, 1.5~3h of weight (hourly) space velocity (WHSV)-1。
The inventive method compared with prior art, with advantages below：
(1) heavy constituent that the inventive method cuts out heavy aromatics carries out selective hydrogenation open loop, it is ensured that two-stage catalytic The stability of agent.
(2) light component that heavy aromatics is cut out in the inventive method does not enter selective hydrogenation reactor, reduces BTX etc. The supersaturation of mononuclear aromatics, improves added value of product and liquid yield.
(3) the heavy aromatics cutting step involved by the inventive method is simple and easy to apply, and because light component is less, cost increase Very little.
Brief description of the drawings
Fig. 1 is produced the process chart of the method for the high-knock rating gasoline rich in BTX for the present invention by heavy aromatics.
In figure, 1 attaches most importance to aroamtic hydrocarbon raw material, and 2 be light component, and 3 be heavy constituent；4 be new hydrogen, and 5 be the production rich in monocyclic heavy aromatics Thing, 6 be mixed oil and gas, and 7 be recycle hydrogen, and 8 be the lighting product rich in BTX, and I is fractionating column, and II is selective hydrogenation Device, III is lighting reactor, and IV is gas-liquid separator.
Embodiment
Below in conjunction with the accompanying drawings and specific implementation row the inventive method is described further.
The present invention is produced to react to react in fixed bed hydrogenation in the method for the high-knock rating gasoline rich in BTX by heavy aromatics and filled Put middle progress.Heavy aromatics raw material 1 enters in fractionating column I, is divided into light component 2 and heavy constituent 3 with 218 DEG C；Heavy constituent 3 and new hydrogen 4 Laggard selectable hydrogenation reactor II is mixed with recycle hydrogen 7 and occurs selective hydrogenation (open loop) reaction, and generation is rich in monocyclic heavy The product 5 of aromatic hydrocarbons；Product 5 and light component 2 rich in monocyclic heavy aromatics enter lighting reactor III after mixing, and occur hydrogenation and split The reaction such as change and transalkylation, generates mixed oil and gas 6；Mixed oil and gas 6 enter in gas-liquid separator IV, and liquid phase is rich in BTX's Lighting product 8, hydrogen is isolated from the gas phase for containing dry gas, liquefied gas to be used to circulate as recycle hydrogen 7, dry gas, liquefaction Gas is produced.Lighting product 8 rich in BTX can be used for extracting BTX, can also be used as high octane gasoline component.
Comparative example 1 and the embodiment of comparative example 2 attach most importance to aroamtic hydrocarbon raw material 1 without fractionating column I, mixed with new hydrogen 4 and recycle hydrogen 7 Close, without selective hydrogenation reactor II, be directly entered lighting reactor III；The embodiment of comparative example 3 is that heavy aromatics is former Material is directly mixed with new hydrogen 4 and recycle hydrogen 71 without fractionating column I, after sequentially enter selective hydrogenation reactor II and lighting Reactor III.
It is involved in the present invention to be defined as follows：
Below by embodiment, the present invention is further elaborated.
Reactor II loads selective hydrocatalyst, the dress lightening catalyst of reactor III, selective hydrocatalyst It is Y molecular sieve and alumina load 0.1%Pt with lightening catalyst, wherein selective hydrocatalyst molecular sieve content is 30%, lightening catalyst molecular sieve content 70%.
Heavy aromatics property used such as table 1, table 2.As can be seen that raw material end boiling range it is very heavy, condensed-nuclei aromatics content close to 50%, But wherein still containing more than 40% monocyclic heavy aromatics.Because condensed-nuclei aromatics content is high, lighting condition is inevitable more harsh, if The monocyclic heavy aromatics in this part is together processed, and is necessarily had substantial amounts of monocyclic heavy aromatics and is saturated to cycloalkane and loses.
The heavy aromatics boiling range of table 1
The heavy aromatics hydrocarbon system of table 2 constitutes
Hydro carbons is other Percentage composition
Alkane 2.5
One cycloalkane 5.3
Bicyclic alkane 0.1
Three cycloalkane 0
Total cycloalkane 5.4
Total saturated hydrocarbons 7.9
Alkylbenzene 23.5
Indane or naphthane 14.9
Indene 4.5
Total mononuclear aromatics 42.9
Naphthalene 0.3
Naphthalenes 15.0
Acenaphthene class 15.8
Acenaphthylene class 10.0
Total double ring arene 41.1
Thrcylic aromatic hydrocarbon 8.1
Total aromatic hydrocarbons 92.1
Summation 100
Embodiment and comparative example condition such as table 3.
The reaction condition of table 3
Embodiment and comparative example experimental result are shown in Table 4.
The embodiment of table 4 and comparative example 1-3 experimental result (units：%)
As can be seen from Table 4, the comparative example 1 of a step lighting method is poor to heavy constituent conversion capability, and catalyst is unstable Fixed, the condition does not have practical value.Improve the comparative example 2, C of pressure10 +Conversion ratio is significantly improved, and catalyst is also maintained preferably Stability, but because pressure is improved, part mononuclear aromatics is hydrogenated saturation and then open loop cracking, generates and largely be difficult to store With the dry gas, liquefied gas utilized, liquid is received low；Comparative example 3 employs two-stage method, and catalyst stability is better than a step lighting method, C10 +Still there is very high BTX selectivity, liquid is received when conversion ratio is higher>90%.C in the raw material of comparative example 210 +Although conversion ratio with Comparative example 3 is more or less the same, but combines C in liquid receipts comprehensive analysis, the raw material of comparative example 210 +Have quite a few generate a large amount of dry gas, Liquefied gas, causes aromatic hydrocarbons loss more；And the liquid of comparative example 3 receives high, C10 +More it is converted into the light aromatics such as BTX and stays in liquid In phase product, it is clear that the good economy performance of comparative example 3 is in comparative example 2.Using the embodiment of the method for the invention, catalyst stability Preferably, C10 +Conversion ratio, BTX selectivity and liquid yield also highest.
It can be seen from experimental data the inventive method can Efficient Conversion heavy aromatics be the high-knock rating gasoline rich in BTX, Have benefited from the fractionation processing of raw material, reduce aromatic hydrocarbons loss, reduce hydrogen consumption and dry gas, liquefied gas yield, improve BTX yield And catalyst stability, it is a kind of heavy aromatics lightening method of optimization.

Claims (3)

1. a kind of method that the high-knock rating gasoline rich in BTX is produced by heavy aromatics, it is characterised in that：Comprise the following steps：
(1) heavy aromatics is cut into light component based on monocyclic heavy aromatics and rich in condensed-nuclei aromatics with 218 DEG C of cut points first Heavy constituent；
(2) heavy constituent enters the first stage reactor, selective hydrogenation saturation and open loop, generates lighting product；
(3) product of step (2) is mixed with the light component in step (1), into the second stage reactor, is hydrocracked and is turned with alkyl Move, gasoline fraction of the generation rich in BTX, by-product dry gas, liquefied gas；
Wherein described heavy aromatics is the single multi- PAH that carbon number is more than or equal to nine, and monocyclic heavy aromatics is to comprise only one The heavy aromatics of phenyl ring, condensed-nuclei aromatics is the heavy aromatics containing two and above phenyl ring.
2. in accordance with the method for claim 1, it is characterised in that the reaction of described selective hydrogenation saturation and ring-opening reaction Condition is：350~400 DEG C of reaction temperature, 3~6MPa of reaction pressure, 0.5~1.5h of weight (hourly) space velocity (WHSV)-1, hydrogen hydrocarbon volume ratio 500~ 1000。
3. in accordance with the method for claim 1, it is characterised in that the described reaction bar being hydrocracked with transalkylation reaction Part is：380~430 DEG C of reaction temperature, 2~4MPa of reaction pressure, 1.5~3h of weight (hourly) space velocity (WHSV)-1。
CN201710461288.6A 2017-06-19 2017-06-19 A kind of method that the high-knock rating gasoline rich in BTX is produced by heavy aromatics Pending CN107286989A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201710461288.6A CN107286989A (en) 2017-06-19 2017-06-19 A kind of method that the high-knock rating gasoline rich in BTX is produced by heavy aromatics

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201710461288.6A CN107286989A (en) 2017-06-19 2017-06-19 A kind of method that the high-knock rating gasoline rich in BTX is produced by heavy aromatics

Publications (1)

Publication Number Publication Date
CN107286989A true CN107286989A (en) 2017-10-24

Family

ID=60096613

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201710461288.6A Pending CN107286989A (en) 2017-06-19 2017-06-19 A kind of method that the high-knock rating gasoline rich in BTX is produced by heavy aromatics

Country Status (1)

Country Link
CN (1) CN107286989A (en)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11136512B2 (en) 2019-12-05 2021-10-05 Saudi Arabian Oil Company Two-stage hydrocracking unit with intermediate HPNA hydrogenation step
CN114436736A (en) * 2020-10-19 2022-05-06 中国石油化工股份有限公司 Catalytic reaction system for heavy aromatic hydrocarbon conversion and method for catalyzing heavy aromatic hydrocarbon conversion

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101760239A (en) * 2008-12-24 2010-06-30 中国石油化工股份有限公司 Utilization method of catalytic cracking diesel
CN103121897A (en) * 2011-11-18 2013-05-29 中国石油化工股份有限公司 Method for preparing arene by mixture containing hydrocarbon with condensed rings
CN104357084A (en) * 2014-11-11 2015-02-18 中国海洋石油总公司 Combined process for conversion of C10+ heavy aromatics to light aromatics
CN105378037A (en) * 2013-07-02 2016-03-02 沙特基础工业公司 Process for upgrading refinery heavy residues to petrochemicals

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101760239A (en) * 2008-12-24 2010-06-30 中国石油化工股份有限公司 Utilization method of catalytic cracking diesel
CN103121897A (en) * 2011-11-18 2013-05-29 中国石油化工股份有限公司 Method for preparing arene by mixture containing hydrocarbon with condensed rings
CN105378037A (en) * 2013-07-02 2016-03-02 沙特基础工业公司 Process for upgrading refinery heavy residues to petrochemicals
CN104357084A (en) * 2014-11-11 2015-02-18 中国海洋石油总公司 Combined process for conversion of C10+ heavy aromatics to light aromatics

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11136512B2 (en) 2019-12-05 2021-10-05 Saudi Arabian Oil Company Two-stage hydrocracking unit with intermediate HPNA hydrogenation step
CN114436736A (en) * 2020-10-19 2022-05-06 中国石油化工股份有限公司 Catalytic reaction system for heavy aromatic hydrocarbon conversion and method for catalyzing heavy aromatic hydrocarbon conversion
CN114436736B (en) * 2020-10-19 2024-01-26 中国石油化工股份有限公司 Catalytic reaction system for heavy aromatics conversion and method for catalyzing heavy aromatics conversion

Similar Documents

Publication Publication Date Title
US10508066B2 (en) Methods and systems of upgrading heavy aromatics stream to petrochemical feedstock
US10077220B2 (en) Aromatics production process
CN1726271B (en) Integrated process for aromatics production
US7304193B1 (en) Integrated process for aromatics production
US10876054B2 (en) Olefin and BTX production using aliphatic cracking reactor
CN102037102B (en) Novel system for optimising the production of high octane gasoline and the coproduction of aromatic bases
US10239802B2 (en) Processes and apparatuses for toluene methylation in an aromatics complex
JP2020502138A (en) Process and equipment for aromatic methylation in aromatic complexes
US11279663B2 (en) Methods and systems of upgrading heavy aromatics stream to petrochemical feedstock
CN111808633A (en) Production method of BTX and LPG
KR20010072935A (en) Para-xylene production process
FR3023842A1 (en) PROCESS FOR PRODUCING HIGH PURITY PARAXYLENE FROM XYLENE CUT, METHOD USING SIMUL MOBILE BED SEPARATION UNIT AND TWO ISOMERIZING UNITS, ONE IN GAS PHASE AND THE OTHER IN LIQUID PHASE.
CN103772123B (en) Method for increasing yield of BTX aromatics
CN103880584A (en) Method for combined production of p-xylene
CN107286989A (en) A kind of method that the high-knock rating gasoline rich in BTX is produced by heavy aromatics
CN105085154B (en) Increase production the method for aroamtic hydrocarbon raw material by heavy aromatics inferior
US20160176778A1 (en) Process for conversion of light aliphatic hydrocarbons to aromatics
US10526554B2 (en) Treating C8-C10 aromatic feed streams to prepare and recover trimethylated benzenes
RU2691987C1 (en) Methods for increasing total output of aromatic hydrocarbons and xylenes in complex production of aromatic hydrocarbons
CN101993333B (en) Combined method for increase production of paraxylene in arene production
US9815754B2 (en) Transalkylation/disproportionation or thermal hydrodealkylation hydrocarbon processing methods and systems employing an increased ethylbenzene feed content
US20200283355A1 (en) Methods and systems of upgrading heavy aromatics stream to petrochemical feedstock
CN105085134B (en) The method that aroamtic hydrocarbon raw material is directly produced by heavy aromatics inferior
CN104447159B (en) A kind of C10+the combined technical method of heavy aromatics lighting
RU2638173C1 (en) Method for obtaining benzol

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
CB02 Change of applicant information

Address after: 100010 Chaoyangmen North Street, Dongcheng District, Dongcheng District, Beijing

Applicant after: China Offshore Oil Group Co., Ltd.

Applicant after: CNOOC TIANJIN CHEMICAL RESEARCH & DESIGN INSTITUTE CO., LTD.

Applicant after: CNOOC Energy Development Co., Ltd.

Address before: 100010 Chaoyangmen North Street, Dongcheng District, Dongcheng District, Beijing

Applicant before: China National Offshore Oil Corporation

Applicant before: CNOOC TIANJIN CHEMICAL RESEARCH & DESIGN INSTITUTE CO., LTD.

Applicant before: CNOOC Energy Development Co., Ltd.

CB02 Change of applicant information
RJ01 Rejection of invention patent application after publication

Application publication date: 20171024

RJ01 Rejection of invention patent application after publication