CN102206504B - Separation method of reformate - Google Patents
Separation method of reformate Download PDFInfo
- Publication number
- CN102206504B CN102206504B CN2011101386439A CN201110138643A CN102206504B CN 102206504 B CN102206504 B CN 102206504B CN 2011101386439 A CN2011101386439 A CN 2011101386439A CN 201110138643 A CN201110138643 A CN 201110138643A CN 102206504 B CN102206504 B CN 102206504B
- Authority
- CN
- China
- Prior art keywords
- mol
- tower
- component
- rectifying
- section
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000000926 separation method Methods 0.000 title claims description 11
- 238000000605 extraction Methods 0.000 claims abstract description 27
- 239000012071 phase Substances 0.000 claims abstract description 7
- 125000003118 aryl group Chemical group 0.000 claims abstract description 3
- 239000007791 liquid phase Substances 0.000 claims abstract description 3
- 238000010992 reflux Methods 0.000 claims abstract 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 17
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 15
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical group CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 claims description 9
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 claims description 6
- URLKBWYHVLBVBO-UHFFFAOYSA-N Para-Xylene Chemical group CC1=CC=C(C)C=C1 URLKBWYHVLBVBO-UHFFFAOYSA-N 0.000 claims description 4
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 4
- IVSZLXZYQVIEFR-UHFFFAOYSA-N m-xylene Chemical group CC1=CC=CC(C)=C1 IVSZLXZYQVIEFR-UHFFFAOYSA-N 0.000 claims description 4
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 claims description 4
- QWTDNUCVQCZILF-UHFFFAOYSA-N iso-pentane Natural products CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 claims description 2
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims description 2
- 229940078552 o-xylene Drugs 0.000 claims description 2
- 238000000034 method Methods 0.000 abstract description 23
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 239000006227 byproduct Substances 0.000 abstract 2
- 238000002407 reforming Methods 0.000 abstract 2
- 239000000047 product Substances 0.000 abstract 1
- 239000000470 constituent Substances 0.000 description 4
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 238000005192 partition Methods 0.000 description 3
- 238000001833 catalytic reforming Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 2
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical group [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000011218 segmentation Effects 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to an apparatus and method for separating reformate; reforming C in the oil by adopting a dividing wall rectifying tower5、C6-C7And C8 +Separating three components; the reformed oil from the reforming device enters a dividing wall rectifying tower from the rectifying section of the feeding part and the middle part of the stripping section of the feeding part, and the tower top C5The components are cooled by a condenser and then enter a reflux tank, and part of liquid phase at the bottom of the reflux tank is used as C5The rest of the component products are returned to the common rectifying section at the upper part of the dividing wall rectifying tower as reflux, C6-C7The components are extracted from the middle part of the rectifying section of the side product extraction part and the stripping section of the side product extraction part through gas phase side extraction, and are cooled by condensationThen sent to an aromatic extraction device, and the tower bottom is C8 +Preparing components; the feeding pressure is 0.5MPa , and the operating pressure of the dividing wall rectifying tower is 0.4MPa ; the energy consumption is low, the purity of the C6-C7 component can reach 99.7 percent, the land occupation is reduced by 40 percent, and the equipment is saved by 20 percent.
Description
Technical field
The present invention relates to a kind of equipment and method of separating reformed oil, adopt the rectifying tower with bulkhead separating reformed oil, in single rectifying tower with bulkhead, reformed oil is separated into to C
5, C
6-C
7And C
8 +Three kinds of components.
Background technology
One of important device of catalytic reforming unit refinery, the reformed oil of its production is rich in aromatic hydrocarbons, has an octane value high, olefin(e) centent is low, substantially characteristics such as sulfur-bearing not, can, directly as the high-octane rating blending component of motor spirit, also can be used for producing the aromatic hydrocarbon products such as benzene, toluene and dimethylbenzene.The reformed oil chief component is C
5 +Distillation gasoline, approximately contain 40 various of monomer hydrocarbon components, when producing high-purity benzene, toluene and dimethylbenzene (being called for short B, T, X) product, reformed oil need to be separated into to different components.Because arene extracting process generally can only be processed narrow boiling-point feeding (C
6～C
7), and to C in charging
5The content of component has restriction, otherwise C
5Can in circulation loop, accumulate and final polluted product.Therefore, reformed oil need to be cut into to C
5, C
6-C
7And C
8 +Component, C
6-C
7Produce benzene and toluene product, C through Aromatics Extractive Project
8 +Produce xylol through fractionation again.Traditional separation method is that cascade towers is set, at first in depentanizer by C
5 -Component is in removed overhead, and at the bottom of depentanizer, oil enters de-C
7Tower, tower top cuts out C
6-C
7, at the bottom of tower, be C
8 +Component.This kind of separation method long flow path, equipment is many, and energy consumption is large, and process cost is higher.Its technical process as shown in Figure 1.
Divided wall column (Dividing Wall Column is called for short DWC) is a kind of rectifying tower of complete thermal coupling, can in single tower, realize three or more product separation.U.S. Pat 6927314B1 adopts divided wall column that full fraction naphtha is divided into gently, neutralizes heavy three kinds of cuts, and lighting end and last running admission oil sump carry out blended gasoline, middle cut after the raising octane value is processed in isomerization as gasoline blending component.U.S. Pat 7169267B2 adopts divided wall column by the separating of oil one-tenth lower boiling of cracking of ethylene, mid-boiling point and three kinds of cuts of high boiling point.Use the divided wall column separating reformed oil, at home and abroad be not reported.
Summary of the invention
The equipment and the method that the purpose of this invention is to provide a kind of separating reformed oil.The raw material of processing is the stable reformed oil that catalytic reforming unit is produced.Adopt rectifying tower with bulkhead, make depentanize and de-C
7Operate in a tower and complete.Have that flow process is short, reduced investment, energy consumption is low, floor space is few characteristics.
Distillation operation of the present invention is to carry out in rectifying tower with bulkhead, and rectifying tower with bulkhead is the rectifying device that a kind of medium position at the conventional rectification tower is provided with a dividing plate, and the central dividing plate at right angle setting prevents that the liquid and gas of both sides from occurring laterally to mix.The internal structure of rectifying tower with bulkhead is divided into public rectifying section, charging rectifying section, charging stripping section, sideline product extraction rectifying section, sideline product extraction stripping section and public stripping section.Charging rectifying section and charging stripping section district share a baffle interval, are called charging prefractionation part, charging is carried out to rough segmentation and heat up in a steamer; Sideline product extraction rectifying section and sideline product extraction stripping section share a baffle interval, together with public rectifying section, public stripping section, are called king-tower, carry out light, in the separating of heavy constituent.Top of tower is provided with condenser, is provided with reboiler at the bottom of tower.
The mode that divided wall column sideline product of the present invention adopts gas phase to extract out, to improve product purity.
The present invention has the following advantages:
1. energy consumption is low
Divided wall column is the ideal system structure on thermodynamics, avoided between charging and feed tray the mixed formation of entropy caused because of difference that component forms, also avoided the back-mixing effect of intermediate component simultaneously, there is higher separation efficiency, and in tower, gas phase flow rate is less than conventional two tower flow process gas phase total amounts, for given material, completes same separation task, divided wall column is than less reboiling heat amount and the condensation number of conventional two tower requirementss of process, and general facilities consumption reduces more than 25%.
2. middle component product purity is high
Adopt the lateral line withdrawal function product of rectifying tower, be difficult to reach high purity.Adopt divided wall column rear feeding and product extraction to separate, stoped the remix of separated portion, sideline product adopts gas phase to extract out simultaneously, has reduced heavy constituent and has carried, extraction product (C6-C7 component) purity 99.7%.
3. flow process is short, takes up an area few
The divided wall column flow process only adopts a tower, with traditional cascade towers flow process, compares, and reduces 1 tower and attached auxiliary facility thereof, has simplified flow process, has saved the occupation of land usable floor area, and occupation of land can reduce approximately 40%.
4. reduced investment
The present invention compares with traditional cascade towers flow process, adopts the divided wall column flow process, and major equipment quantity reduces half, and the divided wall column diameter is less than the tower diameter of diameter maximum in the cascade towers flow process, thus can the decrease cost of investment, and the equipment gross investment can save approximately 20%.
The accompanying drawing explanation
Fig. 1 divided wall column process flow diagram.
Wherein, 1, divided wall column, 2, condenser, 3, return tank, 4, reboiler, I, public rectifying section, the rectifying section of II, feeding part, the stripping section of III, feeding part, the rectifying section of IV, sideline product extraction part, the stripping section of V, sideline product extraction part, VI, public stripping section.
Embodiment
The method of separating reformed oil provided by the invention is so concrete enforcement:
The equipment that the method for separating reformed oil of the present invention adopts is divided wall column 1, be that medium position at the conventional rectification tower arranges a vertical partition plate, tower is separated into to the rectifying section II of public rectifying section I, feeding part, the stripping section III of feeding part, the rectifying section IV of sideline product extraction part, stripping section V, six zones of public stripping section VI (as shown in Figure 1) of sideline product extraction part from top to bottom.Public rectifying section I is positioned at the upper space of divided wall column 1 vertical partition plate, is the disengaging zone of light constituent; Rectifying section and the stripping section of the feeding part separated by dividing plate in the middle part of the rectifying section II of feeding part, the stripping section III of feeding part are respectively, the rectifying section II of feeding part, the stripping section III of feeding part form charging prefractionation part; The stripping section V of the rectifying section IV of sideline product extraction part, sideline product extraction part is respectively rectifying section and the stripping section of sideline product extraction part; Public stripping section VI is positioned at the lower space of divided wall column 1 vertical partition plate; Forms king-tower by the rectifying section IV of public rectifying section I, sideline product extraction part, stripping section V, the public stripping section VI of sideline product extraction part, for gently, in and the disengaging zone of heavy constituent; Be provided with condenser 2 at top of tower, condenser 2 is connected with return tank 3; Be provided with reboiler 4 at the bottom of tower.
The reformed oil come from reformer enters divided wall column 1, tower top C from the rectifying section II of feeding part, the stripping section III middle part of feeding part
5Component enters return tank 3 after condenser 2 is cooling, and 3 end of return tank, a liquid phase part was as C
5The component product, all the other return to divided wall column 1 common rectification section zone, top I, C as backflow
6-C
7Component is carried out the extraction of gas phase side line from the rectifying section IV of sideline product extraction part, the stripping section V middle part of sideline product extraction part, delivers to aromatic extraction unit after condensing cooling, at the bottom of tower, is C
8 +Component.Reboiler 4 adopts middle pressure steam as heat source.Feed pressure is 0.5MPa(g), the divided wall column working pressure is 0.4MPa(g).
Adopt divided wall column flow process separating reformed oil.Processing condition are: treatment capacity is 2,000,000 ton/years, and typical feedstock forms in Table 1, and feed pressure is 0.5MPa(g), the bubble point charging.Separation requirement: C
5Component purity is 99%(mol), C
6-C
7Component purity is 99.7%(mol), C
8 +Component purity is 99%(mol).The divided wall column working pressure is 0.4MPa(g), need altogether 82 tower trays.As shown in Figure 1, processing parameter is in Table 2 in technical process.Adopting as can be seen from Table 2 divided wall column to can save energy energy is 26.1%.
Comparative Examples 1
Adopt cascade towers flow process separating reformed oil.Processing condition are: treatment capacity is 2,000,000 ton/years, and typical feedstock forms in Table 1, and feed pressure is 0.5MPa(g), the bubble point charging.Separation requirement: C
5 -Component purity is 99%(mol), C
6-C
7Component purity is 99.7%(mol), C
8 +Component purity is 99%(mol).The depentanizer working pressure is 0.6MPa(g), need altogether 40 tower trays, de-C
7The tower working pressure is 0.05MPa(g), need altogether 60 tower trays.Processing parameter is in Table 2.
Table 1 reformed oil forms
| Component | mol% |
| i-Butane | 0.0001 |
| n-Butane | 0.0081 |
| i-Pentane | 0.0341 |
| n-Pentane | 0.0220 |
| 2-Mpentane | 0.0905 |
| n-Hexane | 0.0407 |
| Benzene | 0.1462 |
| n-Heptane | 0.0186 |
| Toluene | 0.3124 |
| 2-Mheptane | 0.0009 |
| E-Benzene | 0.0481 |
| p-Xylene | 0.0508 |
| m-Xylene | 0.1079 |
| o-Xylene | 0.0672 |
| 124-MBenzene | 0.0456 |
| n-Pentyl-BZ | 0.0068 |
| Amount to | 1.0000 |
Table 2 divided wall column and two tower flow process parameter lists
Claims (1)
1. the separation method of a reformed oil, it is characterized in that: treatment capacity is 2,000,000 ton/years, separation requirement: C
5Component mole purity is 99%, C
6-C
7Component mole purity is 99.7%, C
8 +Component mole purity is 99%, adopts rectifying tower with bulkhead, by the C in reformed oil
5, C
6-C
7And C
8 +Three kinds of components are separated; The reformed oil come from reformer enters rectifying tower with bulkhead, tower top C from the rectifying section of feeding part, the stripping section middle part of feeding part
5Component enters return tank after condenser is cooling, and at the bottom of return tank, a liquid phase part is as C
5The component product, all the other return to rectifying tower with bulkhead top common rectification section, C as backflow
6-C
7Component is carried out the extraction of gas phase side line from the rectifying section of sideline product extraction part, the stripping section middle part of sideline product extraction part, delivers to aromatic extraction unit after condensing cooling, at the bottom of tower, is C
8 +Component; The charging gauge pressure is 0.5MPa, and rectifying tower with bulkhead operation gauge pressure is 0.4MPa;
The component of described reformed oil is: i-Butane0.0001mol%, n-Butane 0.0081mol%, i-Pentane 0.0341 mol%, n-Pentane 0.0220 mol%, 2-Mpentane 0.0905 mol%, n-Hexane 0.0407 mol%, Benzene 0.1462 mol%, n-Heptane 0.0186 mol%, Toluene 0.3124 mol%, 2-Mheptane 0.0009 mol%, E-Benzene 0.0481 mol%, p-Xylene 0.0508 mol%, m-Xylene 0.1079 mol%, o-Xylene 0.0672 mol%, 124-MBenzene 0.0456 mol%, n-Pentyl-BZ 0.0068 mol%,
The processing parameter of described rectifying tower with bulkhead is: tower top pressure 0.4MPa, 85 ℃ of tower top temperatures, 223 ℃ of column bottom temperatures, 82 of stage number, to product reflux than 15.05, reboiler load 35.98MW, tower diameter 5000mm, tower height 50m, C
5Composition flow rate 164.6kmol/h, C
6-C
7Composition flow rate 1542kmol/h, C
8 +Composition flow rate 836.4kmol/h.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011101386439A CN102206504B (en) | 2011-05-26 | 2011-05-26 | Separation method of reformate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011101386439A CN102206504B (en) | 2011-05-26 | 2011-05-26 | Separation method of reformate |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102206504A CN102206504A (en) | 2011-10-05 |
| CN102206504B true CN102206504B (en) | 2013-12-04 |
Family
ID=44695573
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011101386439A Active CN102206504B (en) | 2011-05-26 | 2011-05-26 | Separation method of reformate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102206504B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US10118878B2 (en) | 2016-09-20 | 2018-11-06 | Uop Llc | Process for increasing xylene isomer to benzene ratio |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107699278B (en) * | 2016-08-08 | 2019-10-29 | 中国石化工程建设有限公司 | A kind of product separation method of hydro carbons CONTINUOUS REFORMER |
| CN108239553B (en) * | 2016-12-23 | 2020-06-09 | 中国石油天然气集团有限公司 | Reforming reaction product separation system and method |
| CN111484868A (en) * | 2019-08-22 | 2020-08-04 | 中国石油天然气集团有限公司 | Naphtha fraction device |
| CN112403013B (en) * | 2020-10-28 | 2023-01-10 | 洛阳金达石化有限责任公司 | Fine processing method of crude hexane |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1469765A (en) * | 2000-09-20 | 2004-01-21 | �����ɷ� | Method and device for carrying out the distillative separation of C5+ cuts |
| CN101348412A (en) * | 2007-07-18 | 2009-01-21 | 中国石油化工股份有限公司 | Energy-saving method for phenyl ethylene rectification |
-
2011
- 2011-05-26 CN CN2011101386439A patent/CN102206504B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1469765A (en) * | 2000-09-20 | 2004-01-21 | �����ɷ� | Method and device for carrying out the distillative separation of C5+ cuts |
| CN101348412A (en) * | 2007-07-18 | 2009-01-21 | 中国石油化工股份有限公司 | Energy-saving method for phenyl ethylene rectification |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US10118878B2 (en) | 2016-09-20 | 2018-11-06 | Uop Llc | Process for increasing xylene isomer to benzene ratio |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102206504A (en) | 2011-10-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100513365C (en) | Method of double solvents, benzene substitutive rectification for separating c9 aromatics | |
| CN102206504B (en) | Separation method of reformate | |
| CN104027995B (en) | The method of Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system | |
| CN202107668U (en) | Dividing wall tower for separating reformate | |
| CN103298531A (en) | Dividing wall-type distillation tower for preparing high-purity 2-ethylhexyl-acrylate and preparation method using same | |
| CN109401779B (en) | Method and device for cutting Fischer-Tropsch synthesis light oil by using bulkhead tower | |
| CN104611059A (en) | Method for preparing liquid paraffin, paraffin precursor and lubricant base oil precursor from Fischer-Tropsch synthesis products | |
| CN101381617A (en) | Fractionation method of hydrocarbon mixtures | |
| CN207047164U (en) | A kind of following light component piece-rate systems of reformed oil C5 | |
| CN106661460A (en) | Petrol production method comprising an isomerisation step followed by at least two separation steps | |
| CN110180202A (en) | The production system and production method of a kind of low coloration high boiling aromatic hydrocarbon solvent of width boiling range | |
| EP3942000A1 (en) | Purification of hexane as by-product of an isomerization unit using a dividing wall column | |
| US9738576B2 (en) | Processes and systems for separating streams to provide a transalkylation feed stream in an aromatics complex | |
| CN103910595A (en) | Separation method for mixture system containing C2, C3, C4, C5 and heavy components | |
| CN103641675B (en) | Separation method of isopropylbenzene mixture system | |
| US20180273446A1 (en) | Processes and systems for purification of 1,3-butadiene | |
| EP3027583B1 (en) | Processes and systems for separating streams to provide a transalkylation feed stream in an aromatics complex | |
| CN209940910U (en) | Dividing wall tower rectifying system for separating catalytic reforming depentanized oil | |
| RU2479620C1 (en) | Method of gas separation during catalytic cracking of petroleum direction | |
| CN108239553B (en) | Reforming reaction product separation system and method | |
| RU2287514C1 (en) | Method of preparing benzene and debenzenized high-octane blend | |
| CN1140606C (en) | Recovery method of diesel oil fraction in tower bottom heavy oil of atmospheric fractional tower | |
| CN118146828A (en) | System for separating aromatic hydrocarbon in pyrolysis gasoline | |
| CN111575045B (en) | Method for reducing benzene and increasing aromatic hydrocarbon yield of desulfurized gasoline | |
| RU121504U1 (en) | INSTALLING THE STABILITY OF STABLE WIDE GASOLINE FRACTIONS |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| ASS | Succession or assignment of patent right |
Owner name: CNPC EAST CHINA PROSPECTING DESIGN + RESEARCH INST Owner name: CHINA PETROLEUM +. NATURAL GAS CO., LTD. Free format text: FORMER OWNER: CNPC EAST CHINA PROSPECTING DESIGN + RESEARCH INSTITUTE Effective date: 20111021 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| C53 | Correction of patent of invention or patent application | ||
| CB03 | Change of inventor or designer information |
Inventor after: Shao Wen Inventor after: Liu Chuanqiang Inventor after: Zhao Xingwu Inventor after: Li Xiaona Inventor after: Zhu Daliang Inventor after: Gong Haifeng Inventor before: Shao Wen Inventor before: Liu Chuanqiang Inventor before: Zhao Xingwu Inventor before: Li Xiaona |
|
| COR | Change of bibliographic data |
Free format text: CORRECT: ADDRESS; FROM: 266071 QINGDAO, SHANDONG PROVINCE TO: 100007 DONGCHENG, BEIJING Free format text: CORRECT: INVENTOR; FROM: SHAO WEN LIU ZHUANQIANG ZHAO XINGWU LI XIAONUO TO: SHAO WEN LIU ZHUANQIANGZHAO XINGWU LI XIAONUO ZHU DALIANG GONG HAIFENG |
|
| TA01 | Transfer of patent application right |
Effective date of registration: 20111021 Address after: 100007 Dongcheng District, Dongzhimen, China, North Street, No. 9 Oil Mansion, No. Applicant after: PetroChina Company Limited Co-applicant after: CNPC EAST CHINA DESIGN INSTITUTE Address before: 266071 Shandong province Qingdao City Hua Road No. 2 Applicant before: CNPC EAST CHINA DESIGN INSTITUTE |
|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |