CN102399589A - Method for reducing content of olefin in reformate - Google Patents
Method for reducing content of olefin in reformate Download PDFInfo
- Publication number
- CN102399589A CN102399589A CN2010102831181A CN201010283118A CN102399589A CN 102399589 A CN102399589 A CN 102399589A CN 2010102831181 A CN2010102831181 A CN 2010102831181A CN 201010283118 A CN201010283118 A CN 201010283118A CN 102399589 A CN102399589 A CN 102399589A
- Authority
- CN
- China
- Prior art keywords
- olefin
- alkene
- reforming catalyst
- quality
- continuous
- 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.)
- Granted
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
A method for reducing the content of olefin in reformate comprises steps of: connecting olefin saturated segments in series in a continuous reforming reaction system, using a continuous reforming catalyst as an olefin saturated catalyst, and converting olefin in the reforming product into saturated hydrocarbon. Calculated by using an inorganic oxide support as the reference, the continuous reforming catalyst contains, by weight, 0.1-5.0% of group VIII metal, 0.1-5.0% of group IV A metal and 0.1-5.0% of halogen. According to the method, the continuous reforming and olefin saturated catalysts are integrated as a whole such that the reforming catalyst is used for olefin saturation under the olefin saturation reaction condition, thus avoiding additional catalyst regeneration process of single use of alkene saturation catalyst with other compositions and simplifying operation steps of the technology.
Description
Technical field
The present invention is a kind of method that reduces olefin(e) centent in the reformed oil, specifically, is a kind of method that reduces olefin(e) centent in the CONTINUOUS REFORMER reaction product.
Background technology
CR is that petroleum naphtha is converted into stop bracket gasoline through catalyzed reaction or is rich in the reformate of aromatic hydrocarbons, rich simultaneously important refining of petroleum technology of producing cheap hydrogen.In catforming process; Be rich in the petroleum naphtha of paraffinic hydrocarbons and naphthenic hydrocarbon; Contact with the platiniferous reforming catalyst under certain condition, the main generation reacted as follows: the naphthenic hydrocarbon dehydrogenation is converted into aromatic hydrocarbons, and the paraffin dehydrogenation cyclisation becomes aromatic hydrocarbons; The isomerizing of paraffinic hydrocarbons and naphthenic hydrocarbon, paraffinic hydrocarbons hydrocracking.
According to the difference of catalyst regeneration mode, catalytic reforming process mainly contains three types: half generative reforming, cyclic regeneration are reformed and (regeneration) reformation continuously.CONTINUOUS REFORMER is developed rapidly because of its liquid yield height, hydrogen productive rate height and aromatics yield advantages of higher in recent years, occupies more and more important position in the oil refining in modern times.
In recent years, the reaction conditions of continuous reforming process constantly develops towards direction favourable to thermodynamic(al)equilibrium and that total energy consumption is minimum.At present, the CONTINUOUS REFORMER reaction pressure has dropped to 0.35MPa, and hydrogen/hydrocarbon mol ratio drops to 1～3, and the RON of reformed oil can be up to 105.Along with the raising of CONTINUOUS REFORMER reaction severity, the content of alkene also obviously improves in the reformed oil.
For the reformer of producing gasoline, C
6Cut need advance extraction plant and take off benzene; For the reformer C that produces aromatic hydrocarbons
6, C
7Cut all needs extracting to separate.Because the selectivity of extraction solvent is limited, extract the alkene that contains some amount in the aromatic hydrocarbons out.Olefin(e) centent is high more in the extracting charging, and the olefin(e) centent of extracting out in the aromatic hydrocarbons is also high more, the alkene accumulation in backflow aromatic hydrocarbons, also can occur, has influence on aromaticity content when serious.In addition, alkene also is prone to produce polymerization in extractive process and pollutes extraction solvent, and alkene generation oxidizing reaction generates the heavy corrosion that organic acid causes extraction system equipment simultaneously.If do not remove alkene wherein, also possibly cause the bromine index of aromatic hydrocarbon product and pickling color defective, the bromine index and the copper strip test of solvent oil are defective.
At present, the Technology of company's exploitation both at home and abroad mainly through part cut in the reformed oil or full cut being carried out selective hydrogenation or non-hydro reaction like post-treating methods such as carclazyte absorption, reaches the purpose of olefin(e) centent in the reduction reformed oil.The type of catalyst system therefor is different with regeneration, and technical process is also corresponding to have different forms.
CN1152605A discloses a kind of process for selective hydrogenation of from reformed oil, removing alkene, is in magnetically stabilized bed reactor, makes liquid reformate generate oil and contacts with a kind of ferromegnetism hydrogenation catalyst with hydrogen.Its reaction conditions is: 50～220 ℃ of temperature of reaction, reaction pressure 0.1～3MPa, reaction velocity 2～40 hours
-1, hydrogen/oil ratio 40～150.
CN1250799A discloses a kind of reformed oil olefine saturation hydrogenation method, is included in catalyzer and exists down, and with reformed oil and contacted with hydrogen, the condition of contact is 50～200 ℃ of temperature, and pressure is greater than 0.1MPa, liquid hourly space velocity 0.1～20 hour
-1, hydrogen/oil ratio is greater than 30; Said catalyzer contains a kind of porous carrier materials, a kind of group VIII metal and is selected from one or both the element in boron, the phosphorus; Said group VIII metal exists with the form of amorphous alloy and is carried in the porous carrier materials; The content of group VIII metal and boron and/or phosphorus is 0.1～60 quality %, and the atomic ratio of group VIII metal element and boron and/or phosphorus is 0.5～10.
CN1394937A discloses a kind of reformed oil olefine saturation hydrogenation method, is included in a kind of catalyzer and exists down, and with reformed oil and contacted with hydrogen, the temperature of contact is 200～320 ℃, and pressure is not less than 0.7MPa, and liquid hourly space velocity is 1～8 hour
-1, hydrogen/oil volume ratio is not less than 30.Said catalyzer contains Tungsten oxide 99.999 and/or molybdenum oxide, nickel oxide and the powder blue that loads on the alumina supporter.
CN1448474A discloses a kind of reformed oil selective hydrogenation and olefin hydrocarbon removal catalyzer.This catalyzer contains the precious metal of 0.1～1.0 quality %, is active ingredient, and the basic metal of 0.05～0.50 quality % or earth alkali metal are auxiliary agent, and support of the catalyst is a refractory inorganic oxides.The surface-area of catalyzer is 150～250m
2/ g, pore volume is 0.3～0.8ml/g.150～250 ℃ of temperature of reaction, pressure 1.5～3.0MPa, volume space velocity 2.0～4.0 hours
-1Under the condition, the bromine index of product is less than 100mgBr/100g oil, and aromatic hydrocarbons loses less than 0.5 quality %.
CN101260320A discloses a kind of CONTINUOUS REFORMER gasoline selective hydrogenation and olefin hydrocarbon removal catalyzer and preparation method.The distinguishing feature of this catalyzer is that the noble metal active component is the eggshell type distribution on carrier, and its advantage is to have significantly improved on the one hand the utilization ratio of noble metal active component, has reduced noble metal active components contents and catalyzer cost; Significantly reduce the activity of aromatic hydrogenation on the other hand, improved the selectivity of hydrogenation of olefins, reduced the aromatic hydrogenation loss.
CN1618932A disclose a kind of under conditions of non-hydrogen the method for catalytic refining reformation aromatic hydrocarbon oil.The catalyzer that adopts is a carrier with aluminum oxide or kaolin, and molecular sieve is an active component.Molecular sieve can be used β, Y, SAPO, ZSM-5, SRCY and super stable molecular sieve.Adopt this method catalytic treatment reformation aromatic hydrocarbon oil, 100～300 ℃ of temperature of reaction, reaction pressure 1.0～2.0MPa, air speed 0.5～4.0 hour
-1Under the condition, can effectively remove the trace amounts of olefin in the aromatic hydrocarbons.
CN101474568A discloses a kind of selective hydrogenation and olefin hydrocarbon removal double-metal phosphide Catalysts and its preparation method.The auxiliary agent of this catalyzer is TiO
2Or rare-earth oxide, Primary Catalysts is the phosphide of a kind of transition metal among Mo, W, Fe, Co or the Ni, catalyzer is through preparing its oxidation state precursor temperature programmed reduction(TPR).When promotor and Primary Catalysts mol ratio are 0.01～0.5, can realize selection hydrogenation, the basic free of losses of aromatic hydrocarbons to alkene in the aromatic hydrocarbons.
CN1163879A discloses a kind of method of producing pure aromatics by reformed gasoline, and reformed gasoline selective hydrogenation in first process steps mainly is that non-aromatic hydrocarbons, particularly alkene, diolefine and alkatrienes are by hydrogenation.Thereafter in second process steps, the product that contains aromatic hydrocarbons of the selection hydrogenation that obtains first process steps through extractive distillation and/or liquid-liquid extraction separates into aromatic hydrocarbons and non-aromatic hydrocarbons.
US7304193B1 discloses a kind of method of producing aromatic hydrocarbons such as benzene and p-Xylol; Feed naphtha is earlier through hydrotreatment; Get into reforming reactor again and carry out catalytic reforming reaction; Recapitalization generating oil hydrogenation reactor drum general alkene wherein carries out saturated, and the product with isomerization unit is mixed into separating unit again, separates wherein benzene and YLENE.The saturated processing of alkene wherein can be adopted carclazyte, preferably uses olefins hydrogenation, and this catalyzer is a carrier with highly purified aluminum oxide, nickel-loaded or platinum metals, and content is about 2～40 quality %.Hydrogenation of olefins saturated reaction condition is 20～200 ℃, 0.5～7.0MPa, and the stoichiometric ratio of hydrogen and alkene is 1～5: 1.
A kind of selectivity of disclosing USP5817227 reduces the method for benzene and lightweight unsaturated compound in the hydrocarbon fraction; This method feeds reformed oil to be had at least in the catalytic distillation tower of a hydrogenation catalyst bed; Make lightweight unsaturated compound hydrogenation in the process of rectifying separation saturated; Discharge C from the distillation tower top with benzene
7 +Component is discharged from the bottom.This method also can increase saturated section of hydrogenation at the distillation tower side line, so that extract the distillation component out from side line, carries out hydrogenation and sends distillation tower again back to after saturated and continue to separate the weight component.Used hydrogenation catalyst is nickel catalyzator or the aluminium oxide catalyst that carries platinum.
Summary of the invention
The purpose of this invention is to provide a kind of method that reduces olefin(e) centent in the reformed oil; This method uses conventional petroleum naphtha continuous reforming catalyst as the saturated catalyzer of alkene in the reformed oil; Save the independent regenerative process of olefins hydrogenation, can effectively reduce the olefin(e) centent in the reformed oil.
The method of olefin(e) centent in the reduction reformed oil provided by the invention; Be included in and be connected in series saturated section of alkene in the CONTINUOUS REFORMER reactive system; With the continuous reforming catalyst is olefins hydrogenation; Making the conversion of olefines in the reformate is stable hydrocarbon, and described continuous reforming catalyst comprises with the inorganic oxide carrier being that the content that benchmark calculates is the VIII family metal of 0.1～5.0 quality %, the IV A family metal of 0.1～5.0 quality %, the halogen of 0.1～5.0 quality %.
The inventive method is integrated CONTINUOUS REFORMER and olefins hydrogenation; It is saturated to make reforming catalyst under the olefin saturation condition, be used to alkene; Avoid the additional catalyst regeneration process of olefins hydrogenation of independent other composition of use, simplified the operation steps of technology.
Embodiment
The inventive method is connected in series the olefin saturation device in the continuous reformer reactive system, and the filling continuous reforming catalyst.During reforming reaction; Earlier petroleum naphtha is fed continuous reforming reactor, after the product that last reactor drum flows out is taken the part heat away through interchanger, get into the olefin saturation device; Under continuous reforming catalyst effect and olefin saturation condition, carry out olefin saturation; And then, send into the device of gas-liquid separator and postorder, production purpose product through heat exchange.
The inventive method uses continuous reforming catalyst as the saturated catalyzer of alkene in the reformate; Preferred 0.1～1.0 quality % of the VIII family metal content of described olefins hydrogenation; Preferred 0.1～2.0 quality % of IV A family metal content, preferred 0.5～3.0 quality % of content of halogen.Described olefins hydrogenation is except that containing VIII family metal and IV A family metal; The 3rd metal constituent element that also contains 0.01～5.0 quality %; And can further contain the 4th metal constituent element of 0.01～5.0 quality %, preferred 0.1～2.0 quality % of the content of the 3rd, the 4th metal constituent element.
The described preferred platinum of VIII family metal that is used for the reforming catalyst of olefin saturation of the inventive method, the preferred tin of IV A family metal, the preferred chlorine of halogen.The preferred europium of described the 3rd, the 4th metal constituent element, cerium or titanium.The preferred aluminum oxide of described inorganic oxide carrier, more preferably gama-alumina.
The preparation method of continuous reforming catalyst can be referring to CN1039917C, CN1234455C, CN100338189C, CN1715370A, CN101294102A, CN1696253A etc.
Described continuous reforming catalyst needs to handle through super-dry, reduction before contact raw oil.The reduction of catalyzer can be carried out before catalyzer is packed reactor drum into, also can after catalyzer is packed reactor drum into, carry out.
The reaction pressure that the said alkene of the inventive method is saturated section is 0.3～1.0MPa, preferred 0.35～0.8MPa, and temperature is 100～400 ℃, preferred 200～350 ℃.The volume space velocity that alkene is saturated section is 10～50 hours
-1, preferred 10～40 hours
-1, hydrogen/hydrocarbon mol ratio is 1～20: 1, preferred 2～8: 1.
The used olefin saturation device of the present invention can be moving-bed, and the catalyzer that alkene is saturated section is participated in the circulation and the regeneration of reforming catalyst; Also can be fixed bed, behind the catalyst deactivation that alkene is saturated section, it cemented out that the online feeding equipment through continuous reformer joins to regenerate in the recycle system of continuous reforming catalyst and recovers active continued and use.
Alkene of the present invention can be gone here and there in the back of the last reactor drum of reforming reactor for saturated section; Use without the regenerated reforming catalyst and be olefins hydrogenation; Also can go here and there, use through the regenerated reforming catalyst to be olefins hydrogenation in the front of first reactor drum.
The inventive method is utilized continuous reformer own resources and equipment, only needs to increase an olefin saturation device, and according to interchanger before and after the condition configuration accordingly of olefin saturation, can increase the catalyzer lift technique when needing.
The inventive method is applicable to the olefine saturation hydrogenation of CONTINUOUS REFORMER product, therefore, cooperates continuous reforming process to use.The raw oil of said CONTINUOUS REFORMER can be that virgin naphtha, hydrogen cracking heavy naphtha, hydrogenation coker gasoline, cracking of ethylene gasoline are raffinated oil, catalytically cracked gasoline, also can be the mixture of several kinds of raw materials wherein.The over point of said raw oil is generally 60～95 ℃, and final boiling point is generally 135～180 ℃.The impurity of reforming raw oil requires: sulphur＜0.5 μ g/g, nitrogen＜0.5 μ g/g, arsenic＜1ng/g, lead＜10ng/g, copper＜10ng/g, water＜5 μ g/g.
The temperature of said reforming reaction is 430～560 ℃, preferred 490～530 ℃; Feed volume air speed 0.1～10.0 hour
-1, preferred 0.5～2.0 hour
-1Pressure is 0.3～1.0MPa, preferred 0.35～0.8MPa; Hydrogen/hydrocarbon mol ratio is 1.5～9.0: 1, preferred 1.5～6.0: 1.
Further specify the present invention through instance below, but the present invention is not limited to this.
Comparative Examples 1
By ordinary method four fixed-bed reactor are connected, the conventional continuous reforming catalyst A of filling in first three reactor drum, loading amount is followed successively by 60ml, 90ml, 150ml, and catalyzer is handled in reactor drum super-dry and the reduction before of packing into.Petroleum naphtha shown in the table 1 is fed three reforming reactors successively; Go into high-pressure gas-liquid separator and carry out gas-liquid separation through overcooling is laggard from the effusive material of reforming reactor, the part in the isolated gas circulates through returning first reactor inlet after the compressor boost.Used reforming catalyst composition, reaction conditions and reformation product liquid composition are seen table 2, and wherein aromatics yield is C
5 +The liquid product yield and the product of aromaticity content wherein, the catalyst A active component content is with carrier γ-Al
2O
3For benchmark calculates.
Comparative Examples 2
Method by instance 1 is carried out reforming reaction, and different is to change the reforming reaction condition, and reaction conditions and reformation product liquid composition are seen table 2.
Comparative Examples 3
Adopt the testing apparatus in the Comparative Examples 1, wherein first three reactor drum loads the reforming catalyst B of the single platinum of load on the chloride alumina supporter successively, and its platinum content is 0.5 quality %, and cl content is 1.0 quality % (all being to calculate benchmark with the alumina supporter).Loading amount is followed successively by 60ml, 90ml, 150ml, and last reactor drum is as the olefin saturation device, and filling 15ml catalyst B is as the olefin saturation catalyzer.Petroleum naphtha shown in the table 1 is fed four reactor drums successively; The material that flows out from the 4th reactor drum is gone into high-pressure gas-liquid separator and is carried out gas-liquid separation through overcooling is laggard, and the part in the isolated gas circulates through returning first reactor inlet after the compressor boost.Reaction conditions that reformation and alkene are saturated and final product liquid composition are seen table 3.
Instance 1
Adopt the testing apparatus in the Comparative Examples 1, wherein first three reactor drum loads conventional continuous reforming catalyst A 60ml, 90ml, 150ml successively, and the 4th reactor drum is as the olefin saturation device, and filling 15ml catalyst A is as the olefin saturation catalyzer.Reaction conditions that reformation and alkene are saturated and final product liquid composition are seen table 3.
Instance 2～3
Method by instance 1 is carried out CR and olefin saturation, and different is that the olefins hydrogenation that loads in the 4th reactor drum of instance 2 is 60ml, and the olefin saturation temperature is different with instance 1; Instance 3 first three reforming reactor reaction conditions are identical with Comparative Examples 2, and the olefins hydrogenation that loads in the 4th reactor drum is 15ml.Reaction conditions that reformation and alkene are saturated and final product liquid composition are seen table 3.
Instance 4
Method by instance 1 is carried out CR and olefin saturation; Different is that the catalyzer that loads in four reactor drums is reforming catalyst C, and its platinum content is 0.35 quality %, and tin content is 0.30 quality %; Titanium content is 0.10 quality %, and cl content is that 1.0 quality % are (all with carrier γ-Al
2O
3For benchmark calculates).Reaction conditions that reformation and alkene are saturated and final product liquid composition are seen table 3.
Instance 5
Method by instance 1 is carried out CR and olefin saturation; Different is that the catalyzer that loads in four reactor drums is reforming catalyst D; Its platinum content is 0.33 quality %, and tin content is 0.30 quality %, and europium content is 0.33 quality %; Cerium content is 1.17 quality %, and cl content is that 1.20 quality % are (all with carrier γ-Al
2O
3For benchmark calculates).Reaction conditions that reformation and alkene are saturated and final product liquid composition are seen table 3.
Table 1
Table 2
Table 3
Claims (10)
1. method that reduces olefin(e) centent in the reformed oil; Be included in and be connected in series saturated section of alkene in the CONTINUOUS REFORMER reactive system; With the continuous reforming catalyst is olefins hydrogenation; Making the conversion of olefines in the reformate is stable hydrocarbon, and described continuous reforming catalyst comprises with the inorganic oxide carrier being that the content that benchmark calculates is the VIII family metal of 0.1～5.0 quality %, the IV A family metal of 0.1～5.0 quality %, the halogen of 0.1～5.0 quality %.
2. according to the described method of claim 1, it is characterized in that described continuous reforming catalyst also contains the 3rd metal constituent element of 0.01～5.0 quality %.
3. according to the described method of claim 2, it is characterized in that described continuous reforming catalyst further contains the 4th metal constituent element of 0.01～5.0 quality %.
4. according to the described method of claim 1, it is characterized in that described VIII family metal is a platinum, IV A family metal is a tin, halogen is a chlorine.
5. according to claim 2 or 3 described methods, it is characterized in that described the 3rd, the 4th metal constituent element is selected from europium, cerium or titanium.
6. according to the described method of claim 1, it is characterized in that described inorganic oxide carrier is an aluminum oxide.
7. according to the described method of claim 1, the reaction pressure that it is characterized in that saturated section of alkene is that 0.2～1.0MPa, temperature are 200～350 ℃.
8. according to the described method of claim 1, the volume space velocity that it is characterized in that saturated section of alkene is 10～40 hours-1, and hydrogen/hydrocarbon mol ratio is 2～8: 1.
9. according to the described method of claim 1, it is characterized in that saturated section of described alkene goes here and there behind the last reactor drum of reforming reactor, use without the regenerated reforming catalyst to be olefins hydrogenation.
10. according to the described method of claim 1, it is characterized in that described alkene goes here and there before first reactor drum for saturated section, use through the regenerated reforming catalyst to be olefins hydrogenation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010283118.1A CN102399589B (en) | 2010-09-16 | 2010-09-16 | Method for reducing content of olefin in reformate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010283118.1A CN102399589B (en) | 2010-09-16 | 2010-09-16 | Method for reducing content of olefin in reformate |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102399589A true CN102399589A (en) | 2012-04-04 |
| CN102399589B CN102399589B (en) | 2014-04-30 |
Family
ID=45882251
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201010283118.1A Active CN102399589B (en) | 2010-09-16 | 2010-09-16 | Method for reducing content of olefin in reformate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102399589B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108367262A (en) * | 2015-12-14 | 2018-08-03 | 沙特基础工业全球技术有限公司 | Method for LPG to be converted to one or more higher hydrocarbons |
| CN110064421A (en) * | 2018-01-23 | 2019-07-30 | 中国石油天然气股份有限公司 | A kind of reforming catalyst and preparation method thereof |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1152605A (en) * | 1995-12-20 | 1997-06-25 | 中国石油化工总公司石油化工科学研究院 | Saturation hydrogenating process for removing olefines from reforming produced oil |
| CN1250799A (en) * | 1998-10-13 | 2000-04-19 | 中国石油化工集团公司 | Saturated hydrogenation of olefin of reforming oil |
| CN1394937A (en) * | 2001-07-10 | 2003-02-05 | 中国石油化工股份有限公司 | Reformed oil olefine saturation hydrogenation method |
-
2010
- 2010-09-16 CN CN201010283118.1A patent/CN102399589B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1152605A (en) * | 1995-12-20 | 1997-06-25 | 中国石油化工总公司石油化工科学研究院 | Saturation hydrogenating process for removing olefines from reforming produced oil |
| CN1250799A (en) * | 1998-10-13 | 2000-04-19 | 中国石油化工集团公司 | Saturated hydrogenation of olefin of reforming oil |
| CN1394937A (en) * | 2001-07-10 | 2003-02-05 | 中国石油化工股份有限公司 | Reformed oil olefine saturation hydrogenation method |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108367262A (en) * | 2015-12-14 | 2018-08-03 | 沙特基础工业全球技术有限公司 | Method for LPG to be converted to one or more higher hydrocarbons |
| US10781379B2 (en) | 2015-12-14 | 2020-09-22 | Sabic Global Technologies B.V. | Process for converting LPG to higher hydrocarbon(s) |
| CN110064421A (en) * | 2018-01-23 | 2019-07-30 | 中国石油天然气股份有限公司 | A kind of reforming catalyst and preparation method thereof |
| CN110064421B (en) * | 2018-01-23 | 2021-11-30 | 中国石油天然气股份有限公司 | Reforming catalyst and preparation method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102399589B (en) | 2014-04-30 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101570698B (en) | Method for catalyzing and transforming naphtha | |
| CN103121897B (en) | By the method for the mixture preparing aromatic hydrocarbon containing hydrocarbon with condensed rings | |
| CN101475429B (en) | Method for comprehensive utilization of cracking C4 | |
| CN103121906B (en) | Method for preparing mononuclear aromatics by using polycyclic aromatic hydrocarbon | |
| CN101376823A (en) | Benzin naphtha catalytic reforming method | |
| CN101914387B (en) | Catalysis upgrading method for cracking ethylene by-product carbon-9 | |
| CN103121895A (en) | Method for preparing monocyclic aromatic hydrocarbons by polycyclic aromatic hydrocarbons | |
| CN103382147B (en) | A kind of method improving mixed c 4 utility value | |
| CN106047404B (en) | A kind of combined technical method of poor quality catalytic cracking diesel volume increase high-knock rating gasoline | |
| CN102337153B (en) | Hydrotreatment method of gasoline distillate oil | |
| CN102051228A (en) | Method for producing aromatic hydrocarbon by catalytically reforming hydrogenation naphtha | |
| CN101619239A (en) | Method for hydrotreatment of heavy fraction of pyrolysis gasoline | |
| CN103045304A (en) | Hydrogenation method of C4 fraction containing rich alkynes and dialkenes | |
| CN112007646A (en) | Carbon-tetrahydrocarbon full-hydrogenation catalyst, preparation method thereof and carbon-tetrahydrocarbon hydrogenation method | |
| CN104031679A (en) | Method for production of olefin and aromatic hydrocarbon from naphtha | |
| CN103509600B (en) | A kind of mixed c 4 hydrocarbon aromatizing produces the method for stop bracket gasoline blend component | |
| JP2012255149A (en) | Process for catalytically reforming naphtha | |
| CN103146428A (en) | Full hydrogenation process of unsaturated hydrocarbon fraction | |
| CN103509601A (en) | Method for co-producing propane by virtue of aromatization of C4 hydrocarbon | |
| CN103058814A (en) | Method for producing aromatic hydrocarbon and olefin from liquefied gas | |
| CN102851075B (en) | Catalytic reforming back-end hydrogenation method | |
| CN104031680B (en) | A kind of method of being produced alkene and low benzene content gasoline by petroleum naphtha | |
| CN101322945B (en) | Method for preparing sulphur-containing condensate oil modifying catalyst and use | |
| CN102399589B (en) | Method for reducing content of olefin in reformate | |
| CN102051231B (en) | Process for producing arene through continuous reforming |
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 |