CN1442358A - Coproduction method of diammonium phosphate and monoammonium phosphate and equipment for neutralizing washing liquid - Google Patents
Coproduction method of diammonium phosphate and monoammonium phosphate and equipment for neutralizing washing liquid Download PDFInfo
- Publication number
- CN1442358A CN1442358A CN 02113425 CN02113425A CN1442358A CN 1442358 A CN1442358 A CN 1442358A CN 02113425 CN02113425 CN 02113425 CN 02113425 A CN02113425 A CN 02113425A CN 1442358 A CN1442358 A CN 1442358A
- Authority
- CN
- China
- Prior art keywords
- phosphoric acid
- phosphate
- diammonium phosphate
- production
- drying
- 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
Images
Abstract
A process for preparing diammonium phosphate and ammonium phosphate features that one part of extracted phosphoric acid is used to prepare diammonium phosphate through concentrating, neutralizing, granulating and drying and the other part is used to prepare ammonium phosphate through washing the tail gas generated in neutralizing-granulating steps, neutralizing the washing liquid, concentrating and spraying drying (or granulating and drying). The neutralizing equipment for washing liquid is composed of flash evaporator, reactino lifting up tube and lowering down tube and forced circulating pump.
Description
One, technical field
The invention belongs to phosphorus ammonium production field, particularly the co-production method of diammonium phosphate and monoammonium phosphate and specific equipment.
Two, background technology
The basic skills of phosphorus ammonium production has two kinds, and a kind of is " Phosphoric Acid Concentration method ", a kind ofly is " in and slurry concentrated process "." Phosphoric Acid Concentration method " be earlier the dilute phosphoric acid of extraction is concentrated into desired concn again in and granulating and drying, mainly be to be used for the high-quality phosphorus ore; " in and slurry concentrated process " is earlier the dilute phosphoric acid of extraction to be neutralized into slip with ammonia, slip is concentrated into granulation or powder process behind the desired concn again, both has been applicable to mid low grade phosphate rock, also is applicable to the high-quality phosphorus ore.Western developed country is good because of its phosphorus ore quality, generally adopt " Phosphoric Acid Concentration method " to produce the phosphorus ammonium, thereby China from the Large-scale Phosphorus ammonium production equipment that western countries introduce all is and " Phosphoric Acid Concentration method " supporting device.This kind Large-scale Phosphorus ammonium production equipment software overhead is big, high and the need auxiliary construction Infrastructure of key hardware price, cause investment per unit capacity very high, the business economic benefit is relatively poor, especially the features of DAP production line that adopts the west import equipment to form, since its processing step be Phosphoric Acid Concentration, in and granulation, drying, washing tail gas, so the Phosphoric Acid Concentration operation must be concentrated into 50～52%P with the dilute phosphoric acid of extraction
2O
5More than tail gas is washed, could solve water balance, in satisfying and granulation to the requirement of phosphoric acid concentration, so not only can reduce the ability and the life-span of Phosphoric Acid Concentration equipment, and can influence the stability that production line moves.
Three, summary of the invention
The present invention is directed to the problem that prior art exists, the co-production method of a kind of diammonium phosphate (DAP) with monoammonium phosphate (MAP) is provided,, reduce production costs, improve the stability of production line operation to expand production capacity.
Co-production method provided by the invention is " in and slurry concentrated process " and a kind of combination of " Phosphoric Acid Concentration method ".The part of institute's phosphoric acid extraction is adopted " Phosphoric Acid Concentration method " production diammonium phosphate (DAP), processing step be Phosphoric Acid Concentration, in and granulating and drying; After another part of institute's phosphoric acid extraction is used for washing the tail gas production diammonium phosphate and that the granulating and drying operation is produced, adopt " in and slurry concentrated process " to produce monoammonium phosphate (MAP) again, processing step is the washings neutralization, the multiple-effect slip concentrates, spray-fluidized-bed drying or spray granulating drying.In this co-production method, the processing parameter of each processing step of production diammonium phosphate is as follows: 1, Phosphoric Acid Concentration is 25%～28%P with the extraction gained
2O
5Dilute phosphoric acid is concentrated into 40-44%P
2O
5Concentration; 2, in and granulating and drying: slip pre-neutralization degree is controlled at 1.4～1.5, and ammonification is to degree of neutralization 1.8～1.9 in the tablets press, and water content is controlled at 3～4%, and the dry gas temperature out is controlled at about 90 ℃.The degree of neutralization of tail gas washing liquid is 0.5～0.8.The processing parameter of producing each processing step of monoammonium phosphate is as follows: 1, washings neutralization, and the degree of neutralization of slip is controlled at 1.0～1.05, and water content is controlled at 42～45%; 2, the multiple-effect slip concentrates, and the water content of enriching slurry is controlled at 20～24%; 3, spray-fluidized-bed drying, drying tower inlet temperature are controlled at 120～135 ℃; 4, spray granulating drying, dry gas temperature out should be controlled at 100～110 ℃.
Co-production method provided by the invention when diammonium phosphate device is not driven or broken down, also can be made the raw material production monoammonium phosphate with dilute phosphoric acid.
In order to realize goal of the invention better, this co-production method has also adopted following technical scheme:
1, can add in the washings in the phosphoric acid storage tank sludge liquid or/and the phosphorus-containing waste slag liquid that commodity phosphoric acid, the production of purification of phosphoric acid salt are produced or/and solid content, the higher phosphoric acid sludge liquid of foreign matter content.
2, in the washings and adopt custom-designed pump circulation ammonification evaporation reaction device, this reactor mainly is made up of flashing chamber, reaction upcast, downtake and forced circulation pump, flashing chamber, reaction upcast and downtake connect into the ring type structure, and the entrance end of forced circulation pump is connected with the reaction upcast with downtake respectively with exit end.
3, spray-fluidized-bed drying adopts the high-temperature flue gas the mode direct and heat exchange of air partition of Coalhotairfurnace generation to add warm air.
The present invention has following beneficial effect:
1, " Phosphoric Acid Concentration method " and " in and slurry concentrated process " are organically combined, can realize capacity expansion revamping at short notice, and the investment of capacity expansion revamping is low and phosphorus ammonium output increases considerably the west phosphorus ammonium production line of being introduced.
2, the direct tail gas that is produced with dilute phosphoric acid washing production diammonium phosphate is also with the raw material of this tail gas washing liquid as the production monoammonium phosphate, not only simplified the processing step of production diammonium phosphate, and the terminal that has reduced the Phosphoric Acid Concentration operation concentrates concentration, because the reduction of concentrated phosphoric acid concentration, can improve the thickening equipment ability greatly, prolong the thickening equipment life-span, reduce steam consumption, improve the stability of production line operation.
3, with the tail gas washing liquid be raw material, adopt " in and slurry concentrated process " to produce monoammonium phosphate and can digest phosphorus-containing waste slag that sludge in the phosphoric acid storage tank and commodity phosphoric acid, the production of purification of phosphoric acid salt produced and solid content, higher phosphoric acid and the sludge of foreign matter content, both made full use of resource, can reduce product cost, environment purification again.
4, in the washings and used pump circulation ammonification evaporation reaction device not only the reaction process stable operation, shockproof, react completely, ammonia loss is little; and be reflected at closed system and finish; and it is concentrated its reaction heat to be used for slip; thereby help improving the stability of production line operation; cut down the consumption of energy and invest, the protection environment.
5, the air heating mode efficient height of spray-fluidized-bed drying is compared with traditional steam-heated cal(l)andria, and is capable of reducing energy consumption about 20%, in addition, also has advantages such as facility compact, flue dust be little, safe and reliable concurrently.
Four, description of drawings
Fig. 1 is a kind of process flow sheet of the co-production method of diammonium phosphate proposed by the invention and monoammonium phosphate;
Fig. 2 is another process flow sheet of the co-production method of diammonium phosphate proposed by the invention and monoammonium phosphate;
Fig. 3 is a kind of structure iron of pump circulation ammonification evaporation reaction device;
Fig. 4 be the high-temperature flue gas that produces of Coalhotairfurnace directly and the synoptic diagram of air partition heat exchange.
Five, embodiment
Embodiment 1:
Present embodiment is that the throughput of former features of DAP production line is 600,000 tons/year to the transformation of the features of DAP production line of introducing, and after transforming, throughput is 800,000 tons/year, 600,000 tons/year of wherein granular diammonium phosphate, 200,000 tons/year of powdery monoammonium phosphates.Improved technical process as shown in Figure 1, phosphoric acid extraction is 400,000 tons, with 300,000 tons of " concentrated phosphoric acid method " production diammonium phosphate that adopt the original production lines wherein, with wherein 100,000 tons be used to wash tail gas that the production diammonium phosphate produced and be raw material with this tail gas washing liquid, adopt " in and slurry concentrated process " to produce powdery monoammonium phosphate.The processing step of production diammonium phosphate comprise successively Phosphoric Acid Concentration, in and granulating and drying; Phosphoric Acid Concentration is to be that to be concentrated into concentration be 42% concentrated phosphoric acid for 28% dilute phosphoric acid with concentration; In and the processing parameter of granulating and drying be: ammonification goes out tablets press water content 3%, 90 ℃ of dry gas temperature outs to degree of neutralization 1.8 in the slip pre-neutralization degree 1.45, tablets press.Add the sludge liquid of phosphoric acid storage tank and the phosphorus-containing waste slag liquid that commodity phosphoric acid, the production of purification of phosphoric acid salt are produced in the washings, with this raw material as the production monoammonium phosphate.The processing step of producing powdery monoammonium phosphate comprises that successively washings neutralization, two effect slips concentrate, spray-fluidized-bed drying; The washings neutralization, the slip degree of neutralization is controlled at 1.03, and water content is controlled at 44%, and the equipment of employing is pump circulation ammonification evaporation reaction device, as shown in Figure 3; Two imitate the concentrated solvent or diluent slurry with moisture 44% of slip is concentrated into moisture 22% enriching slurry; Spray-fluidized-bed drying is finished in spray-drying tower, the high-temperature flue gas that the drying medium ambient air is sent recuperative furnace and Coalhotairfurnace generation to by gas blower directly carries out the heat exchange of air partition, as shown in Figure 4, enter drying tower bottom after the heated air pressurized and finish drying powdery monoammonium phosphate, 130 ℃ of air inlet temperature of stabilizer, 60 ℃ of tower exit temperatures.The powdery monoammonium phosphate product that present embodiment is produced: N11%, effectively P
2O
552%, H
2The granular diammonium phosphate product of O2%: N18%, effectively P
2O
546%, H
2O1.5%.
Embodiment 2:
Present embodiment is newly-built diammonium phosphate, monoammonium phosphate coproduction production line, and technical process as shown in Figure 2.80% of phosphoric acid extraction is adopted " concentrated phosphoric acid method " production diammonium phosphate, rest part is used to wash tail gas that the production diammonium phosphate produced and is raw material, adopt " in and slurry concentrated process " to produce granular monoammonium phosphate with this tail gas washing liquid.It is dry that the processing step of production diammonium phosphate comprises Phosphoric Acid Concentration successively, material is made in neutralization; Phosphoric Acid Concentration is to be that to be concentrated into concentration be 42% concentrated phosphoric acid for 25% dilute phosphoric acid with concentration; In and the processing parameter of granulating and drying be: ammonification goes out tablets press water content 3.5%, 90 ℃ of dry gas temperature outs to degree of neutralization 1.8 in the slip pre-neutralization degree 1.5, tablets press.Add solid content, the higher phosphoric acid sludge liquid of foreign matter content in the washings, with this raw material as the production monoammonium phosphate.The processing step of producing granular monoammonium phosphate comprises that successively washings neutralization, triple effect slip concentrate, spray granulating is dry; The washings neutralization, the slip degree of neutralization is controlled at 1.05, and water content is controlled at 45%, and equipment is pump circulation ammonification evaporation reaction device, as shown in Figure 3; The solvent or diluent slurry that the triple effect slip concentrates moisture 45% is concentrated into moisture 24% enriching slurry; The spray granulating drying, 100 ℃ of dry gas temperature outs.The granular monoammonium phosphate product N10.5% that present embodiment is produced, effectively P
2O
545%, H
2O2%; Granular diammonium phosphate product N16%, effectively P
2O
546%, H
2O1.5%.
Claims (6)
1, the co-production method of a kind of diammonium phosphate and monoammonium phosphate, it is characterized in that with the part of institute's phosphoric acid extraction adopt Phosphoric Acid Concentration, in and granulating drying technology step production diammonium phosphate, after another part of institute's phosphoric acid extraction is used for washing the tail gas production diammonium phosphate and that the granulating and drying operation is produced, adopt again that washings neutralization, multiple-effect slip concentrate, spray-fluidized-bed drying or spray granulating drying process step produce monoammonium phosphate.
2, the co-production method of diammonium phosphate according to claim 1 and monoammonium phosphate is characterized in that Phosphoric Acid Concentration is that the dilute phosphoric acid that will extract gained is concentrated into 40～44%P
2O
5Concentration.
3, according to the co-production method of claim 1 or 2 described diammonium phosphate and monoammonium phosphate, it is characterized in that can adding in the washings in the phosphoric acid storage tank sludge liquid or/and the phosphorus-containing waste slag liquid that commodity phosphoric acid, the production of purification of phosphoric acid salt are produced or/and solid content, the higher phosphoric acid sludge liquid of foreign matter content.
4, the co-production method of diammonium phosphate according to claim 1 and 2 and monoammonium phosphate is characterized in that the high-temperature flue gas the mode direct and heat exchange of air partition that spray-fluidized-bed drying adopts Coalhotairfurnace to produce adds warm air.
5, the co-production method of diammonium phosphate according to claim 3 and monoammonium phosphate is characterized in that the high-temperature flue gas the mode direct and heat exchange of air partition that spray-fluidized-bed drying adopts Coalhotairfurnace to produce adds warm air.
6, a kind of designed pump circulation ammonification evaporation reaction device of washings neutralization procedure that aims at, comprise flashing chamber (1), reaction upcast (2), downtake (4), flashing chamber, reaction upcast and downtake connect into the ring type structure, it is characterized in that also comprising forced circulation pump (3), the entrance end of this pump is connected with the reaction upcast with downtake respectively with exit end.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02113425 CN1235794C (en) | 2002-03-06 | 2002-03-06 | Coproduction method of diammonium phosphate and monoammonium phosphate and equipment for neutralizing washing liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02113425 CN1235794C (en) | 2002-03-06 | 2002-03-06 | Coproduction method of diammonium phosphate and monoammonium phosphate and equipment for neutralizing washing liquid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1442358A true CN1442358A (en) | 2003-09-17 |
| CN1235794C CN1235794C (en) | 2006-01-11 |
Family
ID=27793338
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 02113425 Expired - Fee Related CN1235794C (en) | 2002-03-06 | 2002-03-06 | Coproduction method of diammonium phosphate and monoammonium phosphate and equipment for neutralizing washing liquid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1235794C (en) |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1309658C (en) * | 2003-10-24 | 2007-04-11 | 四川大学 | Method of processing waste gas from ammonium phosphate plate into slurry for two-purpose utilization |
| CN1331749C (en) * | 2004-07-23 | 2007-08-15 | 四川大学 | Tech. for ammoniating integration of acid material fluidifying |
| CN100371238C (en) * | 2006-06-16 | 2008-02-27 | 四川川大中德环保技术有限公司 | Method for producing diammonium phosphate by concentrating acid slime, and secondary ammoniation reactor |
| CN101837964A (en) * | 2010-04-29 | 2010-09-22 | 合肥国轩高科动力能源有限公司 | Preparation method of ammonium dihydrogen phosphate by utilizing ammonia generated when producing lithium iron phosphate |
| CN101734954B (en) * | 2009-12-31 | 2012-04-18 | 瓮福（集团）有限责任公司 | Method for producing granular monoammonium phosphate with diammonium phosphate device |
| CN101734951B (en) * | 2009-12-28 | 2012-08-15 | 瓮福（集团）有限责任公司 | Method for regulating nutrients of diammonium phosphate product |
| CN101734952B (en) * | 2009-12-31 | 2012-10-03 | 瓮福（集团）有限责任公司 | Method for changing granular monoammonium phosphate to produce diammonium phosphate by diammonium phosphate device |
| CN102992817A (en) * | 2012-11-24 | 2013-03-27 | 宜都兴发化工有限公司 | Method for producing microelement granular monoammonium phosphate |
| CN101734953B (en) * | 2009-12-31 | 2013-09-11 | 瓮福（集团）有限责任公司 | Method for changing diammonium phosphate to produce granular monoammonium phosphate by diammonium phosphate device |
| CN103318864A (en) * | 2013-06-21 | 2013-09-25 | 江苏绿陵润发化工有限公司 | Ammonium phosphate flash evaporation chamber improved structure |
| CN103435376A (en) * | 2013-07-29 | 2013-12-11 | 山东明瑞化工集团有限公司 | Method and apparatus used for preparing ammonium phosphate fertilizer from phosphoric acid sediment |
| CN106348267A (en) * | 2016-08-29 | 2017-01-25 | 宜都兴发化工有限公司 | Method for producing diammonium phosphate with nitrogen and phosphorus containing wastewater |
| CN110316709A (en) * | 2019-07-04 | 2019-10-11 | 安徽省司尔特肥业股份有限公司 | A kind of technique using MAP Plant production Diammonium phosphate (DAP) |
-
2002
- 2002-03-06 CN CN 02113425 patent/CN1235794C/en not_active Expired - Fee Related
Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1309658C (en) * | 2003-10-24 | 2007-04-11 | 四川大学 | Method of processing waste gas from ammonium phosphate plate into slurry for two-purpose utilization |
| CN1331749C (en) * | 2004-07-23 | 2007-08-15 | 四川大学 | Tech. for ammoniating integration of acid material fluidifying |
| CN100371238C (en) * | 2006-06-16 | 2008-02-27 | 四川川大中德环保技术有限公司 | Method for producing diammonium phosphate by concentrating acid slime, and secondary ammoniation reactor |
| CN101734951B (en) * | 2009-12-28 | 2012-08-15 | 瓮福（集团）有限责任公司 | Method for regulating nutrients of diammonium phosphate product |
| CN101734953B (en) * | 2009-12-31 | 2013-09-11 | 瓮福（集团）有限责任公司 | Method for changing diammonium phosphate to produce granular monoammonium phosphate by diammonium phosphate device |
| CN101734954B (en) * | 2009-12-31 | 2012-04-18 | 瓮福（集团）有限责任公司 | Method for producing granular monoammonium phosphate with diammonium phosphate device |
| CN101734952B (en) * | 2009-12-31 | 2012-10-03 | 瓮福（集团）有限责任公司 | Method for changing granular monoammonium phosphate to produce diammonium phosphate by diammonium phosphate device |
| CN101837964A (en) * | 2010-04-29 | 2010-09-22 | 合肥国轩高科动力能源有限公司 | Preparation method of ammonium dihydrogen phosphate by utilizing ammonia generated when producing lithium iron phosphate |
| CN102992817A (en) * | 2012-11-24 | 2013-03-27 | 宜都兴发化工有限公司 | Method for producing microelement granular monoammonium phosphate |
| CN102992817B (en) * | 2012-11-24 | 2014-09-03 | 宜都兴发化工有限公司 | Method for producing microelement granular monoammonium phosphate |
| CN103318864A (en) * | 2013-06-21 | 2013-09-25 | 江苏绿陵润发化工有限公司 | Ammonium phosphate flash evaporation chamber improved structure |
| CN103435376A (en) * | 2013-07-29 | 2013-12-11 | 山东明瑞化工集团有限公司 | Method and apparatus used for preparing ammonium phosphate fertilizer from phosphoric acid sediment |
| CN106348267A (en) * | 2016-08-29 | 2017-01-25 | 宜都兴发化工有限公司 | Method for producing diammonium phosphate with nitrogen and phosphorus containing wastewater |
| CN106348267B (en) * | 2016-08-29 | 2019-01-29 | 宜都兴发化工有限公司 | A kind of method and device of Nitrogen-and Phosphorus-containing waste water production Diammonium phosphate (DAP) |
| CN110316709A (en) * | 2019-07-04 | 2019-10-11 | 安徽省司尔特肥业股份有限公司 | A kind of technique using MAP Plant production Diammonium phosphate (DAP) |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1235794C (en) | 2006-01-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1235794C (en) | Coproduction method of diammonium phosphate and monoammonium phosphate and equipment for neutralizing washing liquid | |
| CN100558633C (en) | The method for preparing PHOSPHORIC ACID TECH.GRADE, food grade phosphoric acid and industrial monoammonium phosphate with phosphoric acid by wet process | |
| CN103848407B (en) | A kind of production method of monoammonium phosphate | |
| CN100371238C (en) | Method for producing diammonium phosphate by concentrating acid slime, and secondary ammoniation reactor | |
| CN109052354A (en) | Wet process concentrated phosphoric acid defluorinate production technology | |
| CN101717278B (en) | Method for producing diammonium phosphate by concentrating semi-acidic slurry and secondary ammonization and concentration integrated device | |
| CN1872799A (en) | Associated production method by using condensed phosphoric acid to produce diammonium phosphate, and by using condensed acidic feed pulp to produce phosphor ammonium or/and compound fertilizer | |
| CN110606470B (en) | Device for concentrating, resolving and producing hydrogen chloride from hydrochloric acid | |
| CN101857246B (en) | Process method for co-producing ammonium bicarbonate by using coking plant waste | |
| CN203108242U (en) | Double-effect evaporation system used for ammonium sulphate concentration | |
| CN114455544A (en) | Low-energy-consumption hydrochloric acid resolving process | |
| CN102390822B (en) | Method and device for producing phosphoric acid by using tailing eluate | |
| WO2019100499A1 (en) | Method for producing calcium phosphate salt and high-purity gypsum by using hydrochloric acid and phosphate rock | |
| CN104386709A (en) | Urea hydrolysis reactor with waste heat recovery device | |
| CN103708524B (en) | Method for preparing chemical materials by decomposing potassium-bearing rock by fluorosilicic acid cycling method | |
| CN101811683B (en) | Method for producing phosphates with hot-process phosphoric acid device by utilizing waste heat | |
| CN1927704A (en) | Ammonium phosphate preparation method without tail gas | |
| CN213049440U (en) | Black titanium liquid concentration system | |
| CN114956025A (en) | Preparation process of feed-grade monocalcium phosphate | |
| CN108423690B (en) | Method for directly producing solid ammonium sulfate by heat pump flash evaporation stripping deamination | |
| CN218909884U (en) | System for tertiary concentrated phosphoric acid | |
| CN203048600U (en) | Device for recovering heat of slurry-method-based ammonium phosphate production | |
| CN109646977A (en) | A kind of reactive distillation coupled and its preparing the application in formic acid | |
| CN210030052U (en) | Energy-saving sulfuric acid production line | |
| CN220034363U (en) | Liquid ammonium polyphosphate fertilizer apparatus for producing |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| 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: SICHUAN UNIVERSITY Free format text: FORMER OWNER: CHENGDU CHUANDA INST. OF FINE CHEMISTRY Effective date: 20040806 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20040806 Address after: 610065 Sichuan city of Chengdu province moziqiao Applicant after: Sichuan University Address before: 610065 Sichuan city of Chengdu province moziqiao Applicant before: Chengdu Chuanda Inst. of Fine Chemistry |
|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20060111 |