CN102585071A - Method for producing ethylene-propylene copolymer by recycling ethylene and hydrogen in catalytic dry gas in refinery - Google Patents
Method for producing ethylene-propylene copolymer by recycling ethylene and hydrogen in catalytic dry gas in refinery Download PDFInfo
- Publication number
- CN102585071A CN102585071A CN2012100421482A CN201210042148A CN102585071A CN 102585071 A CN102585071 A CN 102585071A CN 2012100421482 A CN2012100421482 A CN 2012100421482A CN 201210042148 A CN201210042148 A CN 201210042148A CN 102585071 A CN102585071 A CN 102585071A
- Authority
- CN
- China
- Prior art keywords
- hydrogen
- ethene
- propylene copolymer
- absorption
- adsorption
- 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
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Landscapes
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
Abstract
The invention belongs to the field of production of ethylene propylene copolymers and relates to a method for producing an ethylene-propylene copolymer by recycling ethylene and hydrogen in catalytic dry gas in a refinery. The method for producing the ethylene-propylene copolymer by recycling the ethylene and the hydrogen in the catalytic dry gas in the refinery comprises the following steps of: extracting ethylene and hydrogen from the catalytic dry gas by using a pressure swing adsorption technology, wherein the purity of obtained ethylene is more than or equal to 85 percent, and the purity of hydrogen is more than or equal to 99 percent; and producing the ethylene-propylene copolymer by using propylene, a catalyst, an aid and extracted ethylene and hydrogen as raw materials. According to the invention, the catalytic dry gas in the refinery is effectively recycled, and application of the propylene polymer in the refinery is enlarged simultaneously. By adopting the method, only a small amount of devices are added, ethylene and hydrogen are not required to be purchased, and the ethylene-propylene copolymer with different properties can be produced; and the method is simple in whole operation process, low in production cost and suitable for industrialized production.
Description
Technical field
The invention belongs to the ethylene propylene copolymer production field, be specifically related to a kind of method of recycling ethene and hydrogen gas production ethylene propylene copolymer in the plant catalytic dry gas.
Background technology
Vestolen PP 7052 (PP) is one type of widely used general-purpose plastics, and its raw material sources are abundant, and goods have good mechanical property, characteristics such as resistance to chemical attack.But domestic most refinery all has the Vestolen PP 7052 production plant at present, and supply exceed demand for Vestolen PP 7052.In addition, there are shortcomings such as poor performance at low temperatures, notch sensitivity be strong in pure PP, thereby has greatly limited its range of application.
And in propylene polymerization processes, add vinyl monomer, can generate broad-spectrum ethylene propylene copolymer; Like the ethylene propylene copolymer of ethylene content between 2～4% (massfractions) is a kind of modified polypropene, and its toughness and transparency all are superior to Vestolen PP 7052, can be used for making fields such as tubing; The ethylene propylene copolymer of ethylene content between 20～50wt% is ethylene-propylene rubber(EPR); This multipolymer has elastomeric character; Can be used as plastic toughening properties-correcting agent; An amount of ethylene-propylene rubber(EPR) is blended in the Vestolen PP 7052, can obtains the modified polypropylene material of different performance, in the modified polypropene widespread use chemical field of these different performances.
Applicant of the present invention is devoted for years to the refinement research in plant catalytic dry gas; A kind of pressure-swing adsorption novel that reclaims ethene and hydrogen from refinery dry gas is disclosed in the CN101371966 patent of application in early stage; This invention adopts transformation to adsorb the placed in-line new technological process of two towers; Improve the utilization ratio of molecular sieve, reduced displacement tolerance, improved product purity; Adopt that ethylene content is greater than 85% in the ethylene product that technology of the present invention reclaims, yield of ethene is greater than 95%; Hydrogen product purity is greater than 99.9%, and hydrogen yield is greater than 90%.Based on this application for a patent for invention, in view of the present Vestolen PP 7052 present situation that supply exceed demand, applicant of the present invention further is devoted to the research that plant catalytic dry gas is produced ethylene propylene copolymer.
Summary of the invention
Technical problem to be solved by this invention provides a kind of method of recycling ethene and hydrogen gas production ethylene propylene copolymer in the plant catalytic dry gas; This method not only effective recycling ethene and the hydrogen in the catalysis drying gas, and efficiently solve the present situation of present refinery Vestolen PP 7052 production surplus.
The invention provides a kind of method of recycling ethene and hydrogen gas production ethylene propylene copolymer in the plant catalytic dry gas, be specially: from catalysis drying gas, extract ethene and hydrogen through pressure swing adsorption, gained ethene purity >=85%, hydrogen purity >=99%; Ethene, hydrogen with propylene, catalyzer, auxiliary agent and extraction is the raw material production ethylene propylene copolymer again.
The concrete steps that the present invention recycles the method for ethene and hydrogen gas production ethylene propylene copolymer in the plant catalytic dry gas are:
The pre-treatment of A, catalysis drying gas: catalysis drying gas is carried out desulfurization, decarburization, deoxidation, dearsenification, deoxygenated nitrogen, takes off heavy hydrocarbon and drying treatment;
B, transformation absorption purification ethene: the pretreated catalysis drying gas of A step gets into adsorption tower and carries out fractionation by adsorption; Adopt the placed in-line flow process of two towers; Its method is each adsorption tower respectively carries out a series adsorption with two other tower in an adsorption cycle a method, and each adsorption tower adsorption process is that the material of absorption for the first time is the non-absorption phase materials of previous adsorption tower absorption, to tackle the easy absorption phase component of the trace that previous adsorption tower penetrates; The yield of sepn process is guaranteed; The absorption second time is that feed product is directly passed through adsorption bed, and allows the easy absorption of part phase materials to penetrate this bed, and to make easy absorption phase materials on sorbent material, reach absorption saturated as far as possible; The easy absorption phase logistics content that separated is fully guaranteed, and the non-absorption after absorption is done the raw material of absorption for the first time to another adsorption tower mutually; Each adsorption tower adsorbs successively, all pressure drop press, along put, product gas replace, vacuumize, all voltage rise pressure, the circulation step that finally boosts; The stripping gas that vacuumizes is ethene;
Hydrogen is carried in C, transformation absorption: process B step is carried the catalysis drying gas behind the ethene, after the interchanger cooling, gets into transformation absorption and carries hydrogen system; Each adsorption tower adsorbs successively, all pressure drops, along put, vacuumize, all voltage rises, the circulation step that finally boosts; Non-absorption in the adsorption process is product hydrogen mutually;
D, the ethene, the hydrogen that obtain with above-mentioned B, C step are raw material, are equipped with propylene, catalyzer, auxiliary agent and prepare ethylene propylene copolymer.
Preferably, in the aforesaid method in the B step processing condition of transformation absorption purification ethene be: adsorptive pressure 0.1～2MPa, preferred 0.7～1.5MPa; Adsorption temp 50～200 degree, preferred 80～150 degree; Displacement pressure 0.01～0.2MPa, preferred 0.02～0.05MPa; Vacuum desorption pressure-0.06～-0.098MPa, preferred-0.07～-0.08MPa; Vacuum desorption temperature 50～200 degree, preferred 80～150 degree.
Preferably, the processing condition that hydrogen is carried in transformation absorption in the C step in the aforesaid method are: adsorptive pressure 0.1～2MPa, preferred 0.7～1.5MPa; Adsorption temp 0～50 degree, preferred 30～40 degree.
Preferably, the pressure-swing absorber number is the 3-32 platform in the aforesaid method, all presses number of times 2-8 time;
Preferably, sorbent material described in the aforesaid method is at least a in the sorbent material of silica type, zeolite molecular sieve class, complex copper system or zeolite molecular sieve one or more modifications in Ag, Cu, K, Ca, Mg, Sr.
When producing ethylene propylene copolymer, the present invention can adopt batchwise polymerization technology or continuous polymerization technique.
The invention has the beneficial effects as follows:
The present invention utilizes pressure swing adsorption from plant catalytic dry gas, to extract qualified ethene and hydrogen, and with this as raw material, produce in existing refinery on the basis of polypropylene plant, only need to add small number of devices and can prepare qualified ethylene propylene copolymer.The inventive method has the following advantages:
1, effective recycling the catalysis drying gas of refinery, promptly therefrom extract to be fit to produce the ethene and the hydrogen of ethylene propylene copolymer, and, enlarged the purposes of crude propylene polymkeric substance simultaneously as the raw material production ethylene propylene copolymer;
2, the present invention is applicable to have and produces Vestolen PP 7052 production equipment factory and refinery, also is suitable for the convenient Vestolen PP 7052 manufacturer that obtains catalysis drying gas;
3, adopt the present invention only need increase a small amount of device, need not buy ethene/hydrogen, promptly can produce ethylene propylene copolymer of different nature;
4, entire operation technology of the present invention is simple, and production cost is low, is fit to suitability for industrialized production.
Embodiment
The concrete steps that the present invention recycles the method for ethene and hydrogen gas production ethylene propylene copolymer in the plant catalytic dry gas are:
The pre-treatment of A, catalysis drying gas: catalysis drying gas is carried out desulfurization, decarburization, deoxidation, dearsenification, deoxygenated nitrogen, takes off heavy hydrocarbon and drying treatment;
B, transformation absorption purification ethene: the pretreated catalysis drying gas of A step gets into adsorption tower and carries out fractionation by adsorption; Adopt the placed in-line flow process of two towers; Its method is each adsorption tower respectively carries out a series adsorption with two other tower in an adsorption cycle a method, and each adsorption tower adsorption process is that the material of absorption for the first time is the non-absorption phase materials of previous adsorption tower absorption, to tackle the easy absorption phase component of the trace that previous adsorption tower penetrates; The yield of sepn process is guaranteed; The absorption second time is that feed product is directly passed through adsorption bed, and allows the easy absorption of part phase materials to penetrate this bed, and to make easy absorption phase materials on sorbent material, reach absorption saturated as far as possible; The easy absorption phase logistics content that separated is fully guaranteed, and the non-absorption after absorption is done the raw material of absorption for the first time to another adsorption tower mutually; Each adsorption tower adsorbs successively, all pressure drop press, along put, product gas replace, vacuumize, all voltage rise pressure, the circulation step that finally boosts; The stripping gas that vacuumizes is ethene;
Hydrogen is carried in C, transformation absorption: process B step is carried the catalysis drying gas behind the ethene, after the interchanger cooling, gets into transformation absorption and carries hydrogen system; Each adsorption tower adsorbs successively, all pressure drops, along put, vacuumize, all voltage rises, the circulation step that finally boosts; Non-absorption in the adsorption process is product hydrogen mutually;
D, the ethene, the hydrogen that obtain with above-mentioned B, C step are raw material, are equipped with propylene, catalyzer, auxiliary agent and prepare ethylene propylene copolymer.
Producing ethylene propylene copolymer by ethylene, propylene among the present invention adopts prior art to get final product.
Embodiment of the present invention to utilize ethene and hydrogen in the plant catalytic dry gas to produce the concrete steps of method of ethylene propylene copolymer following:
1) select a family to have the refinery that produces polypropylene plant;
2) select the plant catalytic dry gas of composition arbitrarily;
3) select pressure-swing absorption apparatus;
4) selectedly carry out the copolymerization of ethylene, propylene with the mode of rhythmic reaction or successive reaction;
5) in polymerization reactor, add the raw material be used to produce ethylene propylene copolymer, catalyzer, auxiliary agent etc., after the polyreaction of certain hour, obtain modified polypropene.
Through embodiment the present invention is specifically described below; It is important to point out that embodiment only is used for further specifying of the present invention; Can not be interpreted as the restriction to protection domain of the present invention, these those skilled in the art can make some nonessential improvement and adjustment according to the present invention.
Embodiment 1 reclaims hydrogen and ethylene production modified polypropene in the catalysis drying gas
Select plant catalytic dry gas for use; Adopt the pressure-swing adsorption novel method described in the application to reclaim ethene and hydrogen in the plant catalytic dry gas, adopting existing method of producing ethylene propylene copolymer again is that raw material is equipped with other auxiliary agents such as propylene again and prepares modified polypropene with the ethene of aforementioned preparation and hydrogen; The catalysis drying gas composition is seen table 1, isolated ethene, and the purity such as the table 2 of hydrogen, the raw material and the proportioning of modified polypropene are as shown in table 3.
Contained component and content (%) in table 1 catalysis drying gas
| Sample | CH 4 | C 2H 6 | C 2H 4 | C 3H 6 | H 2 | CO |
| Catalysis drying gas | 22.9 | 9.8 | 12.9 | 6.1 | 44.3 | 3.9 |
Table 2 adopts the isolated ethene of pressure swing adsorption process, the purity of hydrogen (%)
| C 2H 4 | H 2 | |
| Purity | ≥85 | ≥99.9 |
Table 3 modified polypropene raw material and proportioning (%)
| Raw material | C 2H 4 | H 2 | C 3H 6 |
| Content | 0～50 | 0～5 | 50～100 |
In addition, the mode of embodiment 1 capable of using obtains ethene and hydrogen, produces ethylene-propylene rubber(EPR) and modified polypropylene material through the content of adjustment ethene.
Claims (9)
1. the method for ethene and hydrogen gas production ethylene propylene copolymer in the recycling plant catalytic dry gas is characterized in that, from catalysis drying gas, extracts ethene and hydrogen through pressure swing adsorption, gained ethene purity >=85%, hydrogen purity >=99%; Ethene, hydrogen with propylene, catalyzer, auxiliary agent and extraction is the raw material production ethylene propylene copolymer again.
2. the method for ethene and hydrogen gas production ethylene propylene copolymer in the recycling plant catalytic dry gas according to claim 1, concrete steps are:
The pre-treatment of A, catalysis drying gas: catalysis drying gas is carried out desulfurization, decarburization, deoxidation, dearsenification, deoxygenated nitrogen, takes off heavy hydrocarbon and drying treatment;
B, transformation absorption purification ethene: the pretreated catalysis drying gas of A step gets into adsorption tower and carries out fractionation by adsorption; Adopt the placed in-line flow process of two towers; Its method is each adsorption tower respectively carries out a series adsorption with two other tower in an adsorption cycle a method, and each adsorption tower adsorption process is that the material of absorption for the first time is the non-absorption phase materials of previous adsorption tower absorption, to tackle the easy absorption phase component of the trace that previous adsorption tower penetrates; The yield of sepn process is guaranteed; The absorption second time is that feed product is directly passed through adsorption bed, and allows the easy absorption of part phase materials to penetrate this bed, and to make easy absorption phase materials on sorbent material, reach absorption saturated as far as possible; The easy absorption phase logistics content that separated is fully guaranteed, and the non-absorption after absorption is done the raw material of absorption for the first time to another adsorption tower mutually; Each adsorption tower adsorbs successively, all pressure drop press, along put, product gas replace, vacuumize, all voltage rise pressure, the circulation step that finally boosts; The stripping gas that vacuumizes is ethene;
Hydrogen is carried in C, transformation absorption: process B step is carried the catalysis drying gas behind the ethene, after the interchanger cooling, gets into transformation absorption and carries hydrogen system; Each adsorption tower adsorbs successively, all pressure drops, along put, vacuumize, all voltage rises, the circulation step that finally boosts; The stripping gas that vacuumizes is hydrogen;
D, the ethene, the hydrogen that obtain with above-mentioned B, C step are raw material, are equipped with propylene, catalyzer, auxiliary agent and prepare ethylene propylene copolymer.
3. the method for ethene and hydrogen gas production ethylene propylene copolymer in the recycling plant catalytic dry gas according to claim 2; It is characterized in that; The processing condition of transformation absorption purification ethene are in the said B step: adsorptive pressure 0.1～2MPa, 50～200 ℃ of adsorption temps, displacement pressure 0.01～0.2MPa; Vacuum desorption pressure-0.06～-0.098MPa, 50～200 ℃ of vacuum desorption temperature.
4. the method for ethene and hydrogen gas production ethylene propylene copolymer in the recycling plant catalytic dry gas according to claim 3; It is characterized in that; The preferred processing condition of purification ethene are in the said B step: adsorptive pressure 0.7～1.5MPa, 80～150 ℃ of adsorption temps, displacement pressure 0.02～0.05MPa; Vacuum desorption pressure-0.07～-0.08MPa, 80～150 ℃ of vacuum desorption temperature.
5. the method for ethene and hydrogen gas production ethylene propylene copolymer in the recycling plant catalytic dry gas according to claim 2; It is characterized in that; Transformation absorption is put forward the processing condition of hydrogen and is in the said C step: adsorptive pressure 0.1～2MPa, 0～50 ℃ of adsorption temp.
6. the method for ethene and hydrogen gas production ethylene propylene copolymer in the recycling plant catalytic dry gas according to claim 5; It is characterized in that; Transformation absorption is put forward the preferred processing condition of hydrogen and is in the said C step: adsorptive pressure 0.7～1.5MPa, 30～40 ℃ of adsorption temps.
7. the method for ethene and hydrogen gas production ethylene propylene copolymer is characterized in that in the recycling plant catalytic dry gas according to claim 2, and the pressure-swing absorber number is the 3-32 platform in said B, the C step, all presses number of times 2-8 time.
8. the method for ethene and hydrogen gas production ethylene propylene copolymer in the recycling plant catalytic dry gas according to claim 2; It is characterized in that sorbent material described in the said B step is at least a in the sorbent material of gac class, activated alumina class, silica type, zeolite molecular sieve class, complex copper system or zeolite molecular sieve one or more modifications in Ag, Cu, K, Ca, Mg, Sr.
9. the method for ethene and hydrogen gas production ethylene propylene copolymer is characterized in that in the recycling plant catalytic dry gas according to claim 1 and 2, can adopt batchwise polymerization technology or continuous polymerization technique when producing ethylene propylene copolymer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012100421482A CN102585071A (en) | 2012-02-23 | 2012-02-23 | Method for producing ethylene-propylene copolymer by recycling ethylene and hydrogen in catalytic dry gas in refinery |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012100421482A CN102585071A (en) | 2012-02-23 | 2012-02-23 | Method for producing ethylene-propylene copolymer by recycling ethylene and hydrogen in catalytic dry gas in refinery |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102585071A true CN102585071A (en) | 2012-07-18 |
Family
ID=46474371
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012100421482A Pending CN102585071A (en) | 2012-02-23 | 2012-02-23 | Method for producing ethylene-propylene copolymer by recycling ethylene and hydrogen in catalytic dry gas in refinery |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102585071A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104031682A (en) * | 2014-05-23 | 2014-09-10 | 四川天采科技有限责任公司 | Method and device for separating hydrogen and ethylene from refinery dry gas by shallow condensing adsorption-absorption |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1817919A (en) * | 2006-03-08 | 2006-08-16 | 南京金陵塑胶化工有限公司 | Production and reactor for polypropylene |
| CN101371966A (en) * | 2007-08-23 | 2009-02-25 | 四川省达科特化工科技有限公司 | Pressure-swing adsorption novel art for recovering ethylene and hydrogen from dry gas of oil-extraction plant |
-
2012
- 2012-02-23 CN CN2012100421482A patent/CN102585071A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1817919A (en) * | 2006-03-08 | 2006-08-16 | 南京金陵塑胶化工有限公司 | Production and reactor for polypropylene |
| CN101371966A (en) * | 2007-08-23 | 2009-02-25 | 四川省达科特化工科技有限公司 | Pressure-swing adsorption novel art for recovering ethylene and hydrogen from dry gas of oil-extraction plant |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104031682A (en) * | 2014-05-23 | 2014-09-10 | 四川天采科技有限责任公司 | Method and device for separating hydrogen and ethylene from refinery dry gas by shallow condensing adsorption-absorption |
| CN104031682B (en) * | 2014-05-23 | 2016-07-06 | 四川天采科技有限责任公司 | The shallow enfleurage of oil refinery dry gas is attached-absorption and separation hydrogen, ethylene method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102701896B (en) | Composite solvent for purifying acetylene and purification method thereof | |
| CN110105217B (en) | Device and method for refining battery-grade dimethyl carbonate | |
| Jiang et al. | Potential biosorbent based on sugarcane bagasse modified with tetraethylenepentamine for removal of eosin Y | |
| CN102516006B (en) | Method and device for recovering ethylene in vinyl acetate production process | |
| CN103772126B (en) | Take oil refinery dry gas as the combined method of waste ethylbenzene | |
| CN104558334A (en) | A preparing method of an anti-shock polypropylene special-purpose material with a high melt index | |
| CN109279611B (en) | Method and device for removing impurities in chlorosilane | |
| CN102585071A (en) | Method for producing ethylene-propylene copolymer by recycling ethylene and hydrogen in catalytic dry gas in refinery | |
| CN103073426B (en) | A kind of take storng-acid cation exchange resin as the preparation technology of catalyst synthesizing propylene tert-butyl acrylate | |
| CN107778140B (en) | Purifying method for ethylene glycol adsorption extraction deep dehydration impurity removal | |
| CN104725201A (en) | Method for adsorption, membrane separation and dehydration of polyoxymethylene dimethyl ether | |
| CN113750958B (en) | Granular starch-based carbon material and preparation method and application thereof | |
| CN114605602B (en) | Hierarchical pore covalent organic framework compound and preparation method and application thereof | |
| CN102643156A (en) | Chloroethane purification process | |
| CN105218819A (en) | The preparation method of a kind of sulfurous gas and epoxy compound composition copolymer | |
| CN102516119B (en) | Continuous low-energy consumption acetonitrile refining process | |
| CN104788617A (en) | Method for reducing color number of cyclopentadiene petroleum resin | |
| CN105439823A (en) | Method for synthesizing 3-methyl-3-butene-1-ol | |
| CN105348032A (en) | Technique for producing styrene by alkylating toluene and methanol side chains | |
| CN107163005B (en) | Industrial equipment for producing anhydrous THF by coupling membrane dehydration and molecular sieve adsorption | |
| CN101143939A (en) | Modified method for waste and old plastic | |
| CN106397089B (en) | Method and system for recovering and purifying hexane solvent in ethylene propylene rubber production | |
| CN107051403A (en) | The preparation method of XDI molecularly imprinted solid phase extraction column packing materials | |
| CN216738132U (en) | Metallocene polypropylene raw materials refining plant | |
| CN112973748A (en) | Synthesis method for in-situ preparation of propylene dimerization catalyst by taking ammonia as solvent |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C53 | Correction of patent of invention or patent application | ||
| CB02 | Change of applicant information |
Address after: 610041, No. 3, building 8, 1 North Bauhinia street, Chengdu hi tech Development Zone, Sichuan, 4 Applicant after: SICHUAN DKT ENERGY TECHNOLOGY CO., LTD. Address before: 610041, No. 3, building 8, 1 North Bauhinia street, Chengdu hi tech Development Zone, Sichuan, 4 Applicant before: Sichuan DKT Energy Technology Co., Ltd. |
|
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20120718 |