CN1332742C - Method for supplying catalyst / auxiliary agnet for catalytic cracking unit - Google Patents
Method for supplying catalyst / auxiliary agnet for catalytic cracking unit Download PDFInfo
- Publication number
- CN1332742C CN1332742C CNB200410037925XA CN200410037925A CN1332742C CN 1332742 C CN1332742 C CN 1332742C CN B200410037925X A CNB200410037925X A CN B200410037925XA CN 200410037925 A CN200410037925 A CN 200410037925A CN 1332742 C CN1332742 C CN 1332742C
- Authority
- CN
- China
- Prior art keywords
- catalyst
- pans
- catalytic cracking
- fresh
- 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.)
- Expired - Lifetime
Links
- 239000003054 catalyst Substances 0.000 title claims abstract description 132
- 238000000034 method Methods 0.000 title claims abstract description 38
- 238000004523 catalytic cracking Methods 0.000 title claims abstract description 22
- 238000006243 chemical reaction Methods 0.000 claims abstract description 22
- 239000012752 auxiliary agent Substances 0.000 claims abstract description 11
- 230000003197 catalytic effect Effects 0.000 claims abstract description 6
- 239000003795 chemical substances by application Substances 0.000 claims description 17
- 239000000203 mixture Substances 0.000 claims description 11
- 239000007795 chemical reaction product Substances 0.000 claims description 6
- 238000005243 fluidization Methods 0.000 claims description 6
- 230000035484 reaction time Effects 0.000 claims description 5
- 230000001737 promoting effect Effects 0.000 claims description 2
- 230000000694 effects Effects 0.000 abstract description 11
- 239000002283 diesel fuel Substances 0.000 abstract description 4
- 238000012986 modification Methods 0.000 abstract 1
- 230000004048 modification Effects 0.000 abstract 1
- 239000011369 resultant mixture Substances 0.000 abstract 1
- 230000001502 supplementing effect Effects 0.000 abstract 1
- 239000000047 product Substances 0.000 description 8
- 239000007789 gas Substances 0.000 description 7
- 239000003921 oil Substances 0.000 description 7
- 238000003860 storage Methods 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 150000001336 alkenes Chemical class 0.000 description 4
- 238000005520 cutting process Methods 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 240000007594 Oryza sativa Species 0.000 description 1
- 235000007164 Oryza sativa Nutrition 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 239000002671 adjuvant Substances 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 230000006698 induction Effects 0.000 description 1
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 235000009566 rice Nutrition 0.000 description 1
- 229930195734 saturated hydrocarbon Natural products 0.000 description 1
- 239000011949 solid catalyst Substances 0.000 description 1
- -1 vapour Substances 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to a method for supplementing catalysts/auxiliary agents for a catalytic cracking device. A rated quantity of catalysts enters a catalyst intermediate tank and homogeneously fluidized by leading in steam and/or dry gas; light oil which needs to be modified is injected in the catalyst intermediate tank and is in contact with the catalysts in the tank for reaction under the condition of catalytic conversion; a resultant mixture of oil gas and the catalysts is lifted and injected in the catalytic cracking device through the settling section of a reactor. The method not only enables the activity of fresh catalysts or auxiliary agents to be fully utilized but also creates conditions for the modification of light oil of gasoline, diesel oil, etc.
Description
Technical field
The present invention relates to catalytic cracking unit catalyst/auxiliary agent compensation process.
Background technology
Catalytic cracking is a most important secondary processing process in the petroleum refining industry, and it is the topmost economic benefit contributor of Petrochemical Enterprises, but also is one of device of energy consumption, material consumption maximum simultaneously.
In the material consumption of catalytic cracking unit, catalyst is maximum consumption item.The unit consumption of catalytic cracking unit catalyst is generally 0.3-1.8Kg catalyst/ton raw material, and the device that has surpasses 2kg catalyst/ton raw material.
The method of present catalytic cracking unit fresh makeup catalyst and auxiliary agent, usually take following way: the fresh catalyst that from the fresh catalyst storage tank, takes, enter manually or the auto feed instrument, through weigh, discharging after the blowing air fluidisation, with catalyst transport to the regenerator of FCC apparatus.Equipment fault in automatic gauge how to realize catalyst, the minimizing auto feed process has more patent.Disclose novel, safe solid catalyst charging system as CN2357817A, CN2361371A, be fit to chemical engineering experiment and production; CN2407174A discloses the automatic small-sized charging system of catalytic cracking catalyst; CN1210029A and 97225598.2 has also proposed automatic feeding device; CN2228082A discloses automatic feeding device of combustion adjuvant or the like.
Because the specific activity equilibrium catalyst of fresh catalyst is high a lot, its micro-activity is generally than high 1 5-20 of equilibrium catalyst more than the unit, therefore, in order to guarantee reaction-regenerative process smooth operation, fresh catalyst can not directly be added in the reactor in actual catalytic cracking production process.Usually, fresh catalyst is added in the regenerator earlier, in the presence of higher regeneration temperature and water vapour, original catalyst mix in initiate catalyst and/or auxiliary agent and the regenerator, and after being accompanied by original catalyst and finishing burning process, the catalyst after regeneration is transported to reactive moieties and participates in reaction again.
The compensation process of above-mentioned fresh catalyst commonly used, can satisfy the steadily requirement of control of course of reaction, but shortcoming is also fairly obvious: the higher activity of fresh catalyst is not fully utilized, and fresh catalyst does not also play a role and just earlier forces inactivation under the high-temperature water heat condition of regenerator; The restriction that in regenerator, distributed by catalyst, fresh catalyst might not brought into play any effect and just carried secretly by flue gas and left regenerator, perhaps mixing with other poising agent draws off from regenerator, perhaps is detained in regenerator for a long time, loss of activity just arrives reactor by " commentariess on classics " after very serious.
In addition on the one hand, catalytic cracking need be produced the clean gasoline or the increasing light olefin yield of low alkene, low sulfur content, as ethene, propylene, or high-value product such as increasing output of diesel oil, often be subjected to the influence of major catalyst activity, assistant concentration (reserve) and upgrading or volume increase limited amount.
In sum, do not relate to any catalytic cracking catalyst compensation process in the prior art as yet with the effect of oil product upgrading.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of novel catalytic cracking catalyst or the compensation process of auxiliary agent, the activity of fresh catalyst or auxiliary agent is fully used, and has created condition for the upgrading of light-end products such as vapour, diesel oil.
Method provided by the invention is: the catalyst of rated capacity enters in the catalyst pans, feeds steam and/or dry gas, makes catalyst fluidization even; With the light-end products injecting catalyst pans of need upgrading, make it to contact with a jar interior catalyst and under catalyticing conversioning condition, react; Reacted oil gas and mixture of catalysts are injected catalytic cracking unit through promoting by the reactor settling section.
Compared with prior art, provided by the present inventionly add the high reaction activity and high that agent method had both made full use of fresh catalyst, created advantage for purpose products such as the upgrading of light-end products such as petrol and diesel oil or increased low carbon olefine outputs again.In addition, the agent method that adds provided by the present invention can also reach the effect that reduces catalyst attrition.
The specific embodiment
In the method for the invention, the described catalyst that enters the catalyst pans both can be fresh catalyst or auxiliary agent, also can be equilibrium catalyst, can also be the mixture of said two devices.Wherein, described equilibrium catalyst both can be from the equilibrium catalyst storage tank, also can be directly from regenerator or catalyst cooler.
In the method for the invention, the catalyst of described rated capacity be meant with the catalyst pans and with the weight that adds the catalyst that agent method adapts of the present invention.If the volume of catalyst pans is less, then each weight that adds the catalyst in the jar also should be fewer, for example, can add the 5-50 kilogram at every turn.Vice versa.
In the method for the invention, the fluidisation of catalyst pans inner catalyst and lifting all can be used steam and/or dry gas.Before the light-end products that will need upgrading injected, the beds density in jar was generally 100-500Kg/m
3, preferred 100-400Kg/m
3, its fluidized state is a dense-phase bed.
In the method for the invention, described catalytic conversion reaction condition is meant that reaction temperature is that 200-650 ℃, reaction pressure are that 0.05-0.40Mpa (cutting off), weight (hourly) space velocity (WHSV) are 1-80h
-1, the reaction time is 1-100s, preferred reaction condition is: reaction temperature is that 250-600 ℃, reaction pressure are that 0.1-0.350Mpa (cutting off), weight (hourly) space velocity (WHSV) are 2-70h
-1, the reaction time is 1.5-80s.The concrete reaction condition character of the oil product of upgrading and the purpose of upgrading is as required determined.Those skilled in the art can determine according to the relevant general knowledge of catalytic cracking process.
In order to make reaction atmosphere in the catalyst pans satisfy the requirement of above-mentioned catalytic conversion reaction, the catalyst that enters the catalyst pans runs well the fresh catalyst or auxiliary agent that institute must be additional except keeping catalytic cracking unit, preferably introduce higher regenerative agent of a certain amount of temperature or poising agent, to keep the temperature of pans inner catalyst bed according to the requirement of oil product upgrading.The higher catalyst of temperature can be directly from regenerator, also can be from the catalyst external warmer, or the poising agent jar of the heat of FCC apparatus.In addition, entering the catalyst of catalyst pans can also be from the cold poising agent jar of FCC apparatus.When the catalyst that enters the catalyst pans is a fresh catalyst and during from the mixture of the equilibrium catalyst of regenerator, the two weight ratio is 1: 1-20.When the catalyst that enters the catalyst pans is a fresh catalyst and during from the mixture of the cooled equilibrium catalyst of catalyst external warmer, the two weight ratio is 1: 1-20.When the catalyst that enters the catalyst pans is a fresh catalyst and during from the mixture of the equilibrium catalyst of the poising agent jar of the heat of FCC apparatus, the two weight ratio is 1: 1-20.
In order to make those skilled in the art understand the present invention better, now method provided by the invention is described in detail as follows: the catalyst from fresh catalyst storage tank (and/or poising agent storage tank, regenerator or external warmer) enters the catalyst pans by measuring requirement, feed steam or dry gas, make catalyst fluidization even; Add a certain amount of material that needs upgrading or processing, as gasoline, react certain hour (as 1-100s) down in uniform temperature (as 200-500 ℃) and pressure (as 0.05-0.40Mpa (cutting off)), catalyst rises in the settler of catalytic cracking unit with product, finishes separating of separating of finish and subsequent product with the reaction oil gas of catalytic cracking unit with catalyst.Step-down, the catalyst pans are purged clean back repeat said process.Is continuous for guarantee handling charging and reacted discharging in whole process, and two or more catalyst pans can be set, and makes above-mentioned steps such as agent, reaction and discharging staggered the carrying out between different catalyst pans that advance.In order to guarantee to react temperature required and the needed catalytic amount of material handling, except that the whole fresh catalysts that replenish by daily requirement, insufficient section can be by the catalyst make-up from regenerator, external warmer and equilibrium catalyst storage tank.
The following examples will give further instruction to method provided by the invention, but therefore the present invention is not subjected to any restriction.
Embodiment
This embodiment explanation: adopt catalyst make-up method provided by the present invention can obtain good implementation result.
With working ability is that 1,000,000 tons/year heavy oil FCC device is an example, implements before the catalyst make-up method of the present invention, and the agent of this device consumption is 1.2 kilograms of/ton raw materials, and the consumption of annual fresh catalyst is 1200 tons.After adopting the method for the invention, device agent consumption is reduced to 0.8 kilogram of/ton raw material, and the consumption of annual fresh catalyst is reduced to 800 tons, 400 tons of annual save catalyst.If according to 2.2 ten thousand yuan of calculating of catalyst per ton, only this item can be cut down expenses 8,800,000 yuan.
In addition, in adding the process of agent, utilize the catalyst pans that FCC gasoline is carried out upgrading, the sulphur of FCC gasoline, nitrogen content are obviously reduced, and olefin content in gasoline is reduced to below the 35v%.The concrete operations step is as follows: from fresh dose of the fresh catalyst storage tank with enter in the catalyst pans from the high temperature regeneration agent of the poising agent of equilibrium catalyst storage tank, the regenerator weight ratio according to 1: 1: 2, the jar end, feed steam, makes catalyst fluidization even; With FCC gasoline injecting catalyst pans, making it in reaction temperature is that 440 ℃, reaction pressure are that 0.25Mpa (cutting off), weight (hourly) space velocity (WHSV) are to react under the condition of 10h-1, and the reaction time is 15s; Reacted catalyst is promoted in the FCC reactor settler with reaction oil gas, finishes separating of separating of finish and subsequent product with the reaction oil gas and the catalyst of catalytic cracking unit.Step-down, the catalyst pans are purged clean back repeat said process.Character contrast before and after the FCC gasoline upgrading is referring to table 1.
Table 1
| Gasoline property | Before the upgrading | Behind the upgrading |
| Density (20 ℃), kilogram/rice 3 | 718.6 | 721.3 |
| Octane number | ||
| RON | 89.6 | 90.5 |
| MON | 79.6 | 80.4 |
| Induction period, minute | 266 | 555 |
| Existent gum, milligram/100 milliliters | ＜2.0 | ＜2.0 |
| Sulfur content, ppm | 321 | 165 |
| Nitrogen content, ppm | 156 | 20 |
| Group composition, heavy % | ||
| Saturated hydrocarbons | 34.97 | 51.00 |
| Alkene | 42.89 | 22.68 |
| Aromatic hydrocarbon | 22.14 | 26.32 |
| Boiling range, ℃ | ||
| Initial boiling point | 39 | 40 |
| 10％ | 56 | 57 |
| 50％ | 97 | 99 |
| 90％ | 175 | 177 |
| Do | 199 | 198 |
Claims (7)
1, a kind of catalytic cracking unit catalyst/auxiliary agent compensation process, it is characterized in that with fresh catalyst with from the equilibrium catalyst of the heat of the cooled or FCC apparatus of regenerator or catalyst external warmer by 1: the mixed mixed catalyst of the weight ratio of 1-20 joins in the catalyst pans, feed steam and/or dry gas, make catalyst fluidization even; With the light-end products injecting catalyst pans of need upgrading, make it to contact with a jar interior catalyst and under catalyticing conversioning condition, react; Reacted oil gas and mixture of catalysts are injected catalytic cracking unit through promoting by the reactor settling section.
2,, it is characterized in that before the light-end products that will need upgrading injected, the beds density in jar was 100-500Kg/m according to the method for claim 1
3
3,, it is characterized in that described catalytic conversion reaction condition is meant that reaction temperature is that 200-650 ℃, reaction pressure are that 0.05-0.40Mpa, weight (hourly) space velocity (WHSV) are 1-80h according to the method for claim 1
-1, the reaction time is 1-100s.
4,, it is characterized in that described catalytic conversion reaction condition is meant that reaction temperature is that 250-600 ℃, reaction pressure are that 0.1-0.350Mpa, weight (hourly) space velocity (WHSV) are 2-70h according to the method for claim 3
-1, the reaction time is 1.5-80s.
5,, it is characterized in that the described catalyst that enters the catalyst pans is a fresh catalyst and from the mixture of the equilibrium catalyst of regenerator, and both weight ratios are 1: 1-20 according to the method for claim 1.
6,, it is characterized in that the described catalyst that enters the catalyst pans is a fresh catalyst and from the mixture of the cooled equilibrium catalyst of catalyst external warmer, and both weight ratios are 1: 1-20 according to the method for claim 1.
7,, it is characterized in that the described catalyst that enters the catalyst pans is a fresh catalyst and from the mixture of the equilibrium catalyst of the poising agent jar of the heat of FCC apparatus, and both weight ratios are 1: 1-20 according to the method for claim 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200410037925XA CN1332742C (en) | 2004-05-14 | 2004-05-14 | Method for supplying catalyst / auxiliary agnet for catalytic cracking unit |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200410037925XA CN1332742C (en) | 2004-05-14 | 2004-05-14 | Method for supplying catalyst / auxiliary agnet for catalytic cracking unit |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1695783A CN1695783A (en) | 2005-11-16 |
| CN1332742C true CN1332742C (en) | 2007-08-22 |
Family
ID=35348769
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB200410037925XA Expired - Lifetime CN1332742C (en) | 2004-05-14 | 2004-05-14 | Method for supplying catalyst / auxiliary agnet for catalytic cracking unit |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1332742C (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102049217B (en) * | 2009-10-27 | 2012-09-12 | 中国石油化工股份有限公司 | On-line filling device and method for catalyst |
| CN101811011B (en) * | 2010-04-13 | 2011-09-07 | 中国石油化工集团公司 | Automatic catalyst-feeding method |
| CN103242890B (en) * | 2012-02-09 | 2015-02-18 | 中国石油化工股份有限公司 | Method for feeding supplementary catalyst to fluidized catalytic cracking (FCC) device |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1059163A (en) * | 1990-08-24 | 1992-03-04 | 上海高桥石化公司炼油厂 | The device of automatic catalyst-feeding and technology |
| CN1208432A (en) * | 1996-09-18 | 1999-02-17 | 法国石油公司 | Method and device for descending catalytic cracking by injecting feedstock at an adequate angle on a conditioned catalyst |
| WO2003089546A1 (en) * | 2002-04-18 | 2003-10-30 | Uop Llc | Process and apparatus for upgrading fcc product with additional reactor with catalyst recycle |
-
2004
- 2004-05-14 CN CNB200410037925XA patent/CN1332742C/en not_active Expired - Lifetime
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1059163A (en) * | 1990-08-24 | 1992-03-04 | 上海高桥石化公司炼油厂 | The device of automatic catalyst-feeding and technology |
| CN1208432A (en) * | 1996-09-18 | 1999-02-17 | 法国石油公司 | Method and device for descending catalytic cracking by injecting feedstock at an adequate angle on a conditioned catalyst |
| WO2003089546A1 (en) * | 2002-04-18 | 2003-10-30 | Uop Llc | Process and apparatus for upgrading fcc product with additional reactor with catalyst recycle |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1695783A (en) | 2005-11-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101190416B (en) | Catalytic cracking catalyst and preparation method thereof | |
| WO2020015603A1 (en) | Method, reactor and system for catalytic cracking of hydrocarbon oil | |
| CN107267211A (en) | The processing method and system of a kind of inferior feedstock oil | |
| EP3919589A1 (en) | Method for catalytic conversion of hydrocarbon with downer reactor and device thereof | |
| CN102051199B (en) | Catalytic conversion method for reducing benzene content in gasoline | |
| CN101314732B (en) | Continuous aromatization modification method for hydrocarbons | |
| CN102234535B (en) | Method for processing low-quality heavy oil and simultaneously producing synthetic gas | |
| CN1332742C (en) | Method for supplying catalyst / auxiliary agnet for catalytic cracking unit | |
| CN100523141C (en) | Heavyoil catalytic cracking and gasoline modifying mutual control method and apparatus | |
| CN107267190B (en) | A kind of method of high olefin content gasoline upgrading | |
| US2763596A (en) | Fluid hydroforming process | |
| CN102746887A (en) | Catalytic cracking method | |
| CN103028389B (en) | Subtract sulfur catalyst compositions of additives and preparation method thereof for fluid catalytic cracking | |
| CN210560276U (en) | Device for comprehensively utilizing styrene heavy distillate oil | |
| CN101362964A (en) | Catalytic conversion method for reducing benzene content in gasoline | |
| CN102268290B (en) | Catalytic cracking method and device | |
| CN1333048C (en) | Petroleum hydrocarbon catalytic conversion method | |
| CN102952578B (en) | Catalytic cracking method for increasing light olefin yield | |
| CN102268291A (en) | Catalytic cracking technology and device for reducing olefins in gasoline | |
| CN102453540B (en) | Catalytic conversion method for increasing high octane number gasoline yield | |
| CN102311767B (en) | Gasoline olefin reducing catalytic cracking method and device | |
| US2765263A (en) | Pretreatment process for fluid hydroforming | |
| CN105505454B (en) | A kind of shale oil fluidized catalytic cracking method | |
| CN102453522B (en) | Catalytic conversion method of high-yield high-octane-number gasoline | |
| CN1333050C (en) | Catalysis method for upgrading hydrocarbon oil |
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 | ||
| CX01 | Expiry of patent term |
Granted publication date: 20070822 |
|
| CX01 | Expiry of patent term |