CN102398909A - Method for producing ammonium sulfate by using high-ammonium-nitrogen sulfur-containing high-salinity wastewater - Google Patents
Method for producing ammonium sulfate by using high-ammonium-nitrogen sulfur-containing high-salinity wastewater Download PDFInfo
- Publication number
- CN102398909A CN102398909A CN2010102751558A CN201010275155A CN102398909A CN 102398909 A CN102398909 A CN 102398909A CN 2010102751558 A CN2010102751558 A CN 2010102751558A CN 201010275155 A CN201010275155 A CN 201010275155A CN 102398909 A CN102398909 A CN 102398909A
- Authority
- CN
- China
- Prior art keywords
- solid
- ammonium sulfate
- liquid
- catalyzer
- gac
- 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
Landscapes
- Removal Of Specific Substances (AREA)
- Water Treatment By Sorption (AREA)
- Fertilizers (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The invention relates to a method for preparing ammonium sulfate from high-ammonium-nitrogen sulfur-containing high-salinity wastewater. The method comprises the following steps of: mixing the wastewater with active carbon as well as a catalyst, then aerating by using air or pure oxygen at the temperature of 10-95 DEG C and reacting mixture for 10-720 minutes; performing solid-liquid separation on reacted slurry, wherein solid is mixture of the catalyst and the active carbon and can be continuously used after being regenerated, and the liquid is evaporated, concentrated, crystallized and dried to obtain an ammonium sulfate product; and concentrating and crystallizing mother liquor, returning to aerate, catalyze, oxidize and continuously purify the mother liquor to be used as a material. By adopting the method, the problem of pollution caused to environment by the high-ammonium-nitrogen sulfur-containing high-salinity wastewater is solved; meanwhile, the high-purity ammonium sulfate product is produced; and recycling of waste is realized.
Description
Invention field
The present invention relates to the process method that the low organic wastewater of a kind of high salt utilizes again, particularly relate to the method that a kind of waste water that utilizes high density to contain ammonium, anions containing sulfur prepares ammonium sulfate.
Background technology
In the production process of industries such as metallurgy, chemical industry, chemical fertilizer, food-processing, plating, often produce a large amount of high-salt wastewaters, its total salt concentration often reaches more than 10%, if directly discharging will cause potential harm to environment, therefore must administer it.
At present; The improvement method commonly used of the high-salt wastewater of China's patent report mainly contains: biological degradation method (CN200910191713.X; CN201010170494.X), method for separating and recovering (CN200710167258.0), materialization treatment process (CN200810119250.1; CN200610023287.5, CN200820081752.5), chemistry-biochemistry combination facture (CN200810138217.3) etc.These methods all are to a certain type of waste water, and the range of application that is fit to is separately arranged.
In industries such as metallurgy, chemical industry, chemical fertilizers production, food-processing, plating, there is one type of waste water, is characterized in that salt concn is higher, generally reach more than 10%; Positively charged ion is single in the salt component; Especially the most common with ammonium ion, anion species is more, and is main with the anions containing sulfur of different valence state; Organic content is relatively low, and how exists with the form of dissolving oil.This type waste water lacks enough carbon sources because organic content is low, is inappropriate for biological treatment; On the other hand, because ammonium salt solubleness is high, the difficulty of Separation and Recovery is bigger; Separation costs is higher with respect to value of the product, and the economy of Separation and Recovery is relatively poor, and often with the secondary pollution deposits yields; As after adding alkali ammonia still process, residue waste water still contains the salt and the COD of high density, and environmental exposure is bigger; Materialization treatment process generally need add deposition or the medicament or carry out pyroreaction of flocculating, and cost is high and be difficult to obtain high-valued product, so economy is also relatively poor.
Therefore,, develop that a kind of cost is low, the treatment process of non-secondary pollution, fully reclaim valuable constituent wherein, and make residue waste water reach discharging standards, have great importance for relevant enterprise to the character of this type waste water.
Summary of the invention
The objective of the invention is in order to solve existing high ammonia nitrogen, the high-salt wastewater difficult treatment of sulfur-bearing, problem that processing cost is high; Thereby a kind of method of utilizing this type waste water to adopt absorption oil removing-low-cost catalyzed oxidation purifying high-purity ammonium sulfate is provided, and this method adopts heterogeneous catalyst, and transformation efficiency is high, and product ammonium sulfate purity is high and do not have a high salt high-COD waste water discharging.
Provided by the inventionly utilize high ammonia nitrogen sulfur-bearing high-salt wastewater to prepare the method for ammonium sulfate, comprise the steps:
1) catalyzed oxidation: under 10～95 ℃, catalyzer, gac are dropped in the waste water simultaneously, employing air or pure oxygen aeration also stirred 10～720 minutes, and grease by activated carbon adsorption following chemical reaction is taken place in addition during the aeration:
2) catalyst regeneration: the step 1) post reaction mixture is carried out solid-liquid separation; Wherein solid comprises gac and catalyzer; 200～900 ℃ of blowing air heating 30～600 minutes; Obtain gac and mixture of catalysts, activated carbon adsorptive capacity, catalyst activity are restored at this moment, can directly reuse;
3) evaporative crystallization: the step 1) post reaction mixture is carried out the liquid that solid-liquid separation obtains evaporate, stop evaporation after the crystallization 80%, use whizzer separate solid and liquid;
4) mother liquor refluxes: the liquid that step 3) is obtained turns back to step 1) and proceeds catalytic oxidation treatment;
5) drying: the solid that step 3) is obtained carries out drying, obtains ammonium sulfate product.
In above-mentioned technical scheme, the high-salt wastewater of said high ammonia nitrogen, sulfur-bearing is the trade effluent of Iron and Steel Production, gasification, coal tarization, flue gas desulfurization, grain deep processing, food-processing, plating, chemical fertilizer, the generation of furfural production industry.
In technique scheme; Said catalyzer or heterogeneous catalyst refer to by one or more metal composite in nickel, iron, cobalt, vanadium, chromium, manganese, gold and silver, copper, tin, cadmium, rubidium, titanium, the aluminium after the MOX that the oxygenation roasting generates; Its existence form is a pressed powder, and particle size is 1～1000 μ m.The addition of catalyzer is 0.01%～1% of a wastewater treatment capacity.
In technique scheme, said activated carbon is powdered carbon or granular carbon, and the addition of activated carbon is 0.1%～5% of a wastewater treatment capacity.
Compared with prior art, advantage of the present invention is:
Compare with biological degradation method, present method can be handled the high waste water of ammonia nitrogen concentration, and can access the ammonium sulfate product with sales value.Compare with method for separating and recovering, though present method product is single, need not complicated Crystallization Separation process, nearly all solute all gets into product, and technology is simple and yield is high.Compare with materialization treatment process, present method does not consume medicaments such as flocculation agent, need not high-temperature high-voltage reaction, and lower to equipment requirements, cost is low.Present method has adopted activated carbon adsorption most of organism, and need not to adopt acid-alkali accommodation pH, thereby pollutent indexs such as the COD of evaporation condensed water, ammonia nitrogen all can reach discharging standards, non-secondary pollution.
Description of drawings
Fig. 1 process flow diagram of the present invention
Embodiment
In order to make the object of the invention, technical scheme and advantage clearer, below in conjunction with accompanying drawing and embodiment to further explain of the present invention.
Embodiment 1
With reference to accompanying drawing 1, present embodiment is the method for producing ammonium sulfate with coal gas ammonia process of desulfurization waste water, and concrete technology is following:
1) catalyzed oxidation: get iron, vanadium, the copper of amount of substance and obtain catalyzer through roasting than 1: 1: 3; Drop in the waste water simultaneously at 95 ℃ of catalyzer that will be equivalent to down wastewater flow rate 1%, the gac that is equivalent to wastewater flow rate 0.1%; The employing pure oxygen aeration also stirred 720 minutes; During the aeration in the waste water grease such as dissolved tar following chemical reaction is taken place in addition by activated carbon adsorption:
2) catalyst regeneration: the step 1) post reaction mixture is carried out solid-liquid separation, and wherein solid comprised gac and catalyzer, 900 ℃ of blowing air heating 600 minutes; Obtain gac and mixture of catalysts; Can directly reuse, because catalyst regeneration temperature is higher and the time is longer, the part gac can burn; Therefore need to replenish proper amount of active carbon, make the gac total amount identical with original bulk;
3) evaporative crystallization: the step 1) post reaction mixture is carried out the liquid that solid-liquid separation obtains evaporate, stop evaporation after the crystallization 80%, use whizzer separate solid and liquid;
4) mother liquor refluxes: the liquid that step 3) is obtained turns back to step 1) and proceeds catalytic oxidation treatment;
5) drying: the solid that step 3) is obtained carries out drying, obtains ammonium sulfate product.
Embodiment 2
Present embodiment is the method for producing ammonium sulfate with corn deep processing waste water, and concrete technology is following:
Get amount of substance than 1: 1: 2: 5: 1 nickel, iron, chromium, titanium, aluminium obtain catalyzer through roasting; Drop in the waste water simultaneously at 10 ℃ of catalyzer that will be equivalent to down wastewater flow rate 0.01%, the gac that is equivalent to wastewater flow rate 0.1%; The employing air aeration also stirred 10 minutes; During the aeration in the waste water dissolved corn grease through catalyzed reaction the ion of all sulfur-bearings is converted into sulfate radical in addition by activated carbon adsorption.
Mixture behind the catalytic oxidation is carried out solid-liquid separation; Wherein solid comprises gac and catalyzer, 200 ℃ of blowing air heating 30 minutes, obtains gac and mixture of catalysts; Because catalyst regeneration temperature is lower and the time is shorter; Gac loses seldom, and gac total amount and original bulk are basic identical, can directly reuse.
Mixture behind the catalytic oxidation is carried out the liquid that solid-liquid separation obtains evaporate, stop evaporation after the crystallization 80%, use whizzer separate solid and liquid, with liquid return to catalyzed oxidation step, solid obtains ammonium sulfate product after drying.
Embodiment 3
Present embodiment is the method for producing ammonium sulfate with chemical fertilizers production waste water, and concrete technology is following:
Get amount of substance than 1: 6: 1: 2 cobalt, manganese, cadmium, rubidium obtain catalyzer through roasting; Drop in the waste water simultaneously at 60 ℃ of catalyzer that will be equivalent to down wastewater flow rate 0.3%, the gac that is equivalent to wastewater flow rate 1%; Adopt air aeration also to stir 300 minutes, through catalyzed reaction the ion of all sulfur-bearings is converted into sulfate radical during the aeration.
Mixture behind the catalytic oxidation is carried out solid-liquid separation; Wherein solid comprises gac and catalyzer, 550 ℃ of blowing air heating 240 minutes, obtains gac and mixture of catalysts; Because under this reaction conditions; Gac only has small loss, be supplemented to be equivalent to wastewater flow rate about 1% after, can continue to use.
Mixture behind the catalytic oxidation is carried out the liquid that solid-liquid separation obtains evaporate, stop evaporation after the crystallization 80%, use whizzer separate solid and liquid, with liquid return to catalyzed oxidation step, solid obtains ammonium sulfate product after drying.
Present method is at first utilized the activated carbon adsorption organism, and in same reactor drum, carries out catalytic oxidation, and the sulphur in the waste water all is promoted to+6 valencys, makes in the water solute simplification of trying one's best, thereby is beneficial to the crystallization of product.Present method does not have the high-concentration waste water of effluxing, and need not to carry out a biological disposal upon, and reclaim(ed) sulfuric acid ammonium product has reduced production cost simultaneously, has high economic benefit.
Should be noted that and understand, under the situation that does not break away from the desired the spirit and scope of the present invention of accompanying Claim, can make various modifications and improvement the present invention of above-mentioned detailed description.Therefore, the scope of the technical scheme of requirement protection does not receive the restriction of given any specific exemplary teachings.
Claims (4)
1. one kind is utilized high ammonia nitrogen sulfur-bearing high-salt wastewater to prepare the method for ammonium sulfate, and its step comprises:
1) catalyzed oxidation: under 10～95 ℃, catalyzer, gac are dropped in the waste water simultaneously, employing air or pure oxygen aeration also stirred 10～720 minutes, and grease by activated carbon adsorption following chemical reaction is taken place in addition during the aeration:
2) catalyst regeneration: the step 1) post reaction mixture is carried out solid-liquid separation; Wherein solid comprises gac and catalyzer; 200～900 ℃ of blowing air heating 30～600 minutes; Obtain gac and mixture of catalysts, activated carbon adsorptive capacity, catalyst activity are restored at this moment, can directly reuse;
3) evaporative crystallization: the step 1) post reaction mixture is carried out the liquid that solid-liquid separation obtains evaporate, stop evaporation after the crystallization 80%, use whizzer separate solid and liquid;
4) mother liquor refluxes: the liquid that step 3) is obtained turns back to step 1) and proceeds catalytic oxidation treatment;
5) drying: the solid that step 3) is obtained carries out drying, obtains ammonium sulfate product.
2. according to claim 1, the high-salt wastewater of said high ammonia nitrogen sulfur-bearing is the trade effluent of Iron and Steel Production, gasification, coal tarization, flue gas desulfurization, grain deep processing, food-processing, plating, chemical fertilizer, the generation of furfural production industry.
3. according in the claim 1 1); Said catalyzer or heterogeneous catalyst refer to by one or more metal composite in nickel, iron, cobalt, vanadium, chromium, manganese, gold and silver, copper, tin, cadmium, rubidium, titanium, the aluminium after the MOX that the oxygenation roasting generates; Its existence form is a pressed powder, and particle size is 1～1000 μ m; The addition of catalyzer is 0.01%～1% of a wastewater treatment capacity.
4. according in the claim 1 2), said activated carbon is powdered carbon or granular carbon, the addition of activated carbon is 0.1%～5% of a wastewater treatment capacity.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010275155.8A CN102398909B (en) | 2010-09-08 | 2010-09-08 | Method for producing ammonium sulfate by using high-ammonium-nitrogen sulfur-containing high-salinity wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010275155.8A CN102398909B (en) | 2010-09-08 | 2010-09-08 | Method for producing ammonium sulfate by using high-ammonium-nitrogen sulfur-containing high-salinity wastewater |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102398909A true CN102398909A (en) | 2012-04-04 |
| CN102398909B CN102398909B (en) | 2014-11-05 |
Family
ID=45881624
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201010275155.8A Active CN102398909B (en) | 2010-09-08 | 2010-09-08 | Method for producing ammonium sulfate by using high-ammonium-nitrogen sulfur-containing high-salinity wastewater |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102398909B (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103288286A (en) * | 2013-06-28 | 2013-09-11 | 陕西煤业化工技术研究院有限责任公司 | Catalytic oxidation treatment method for desulfurized waste liquid |
| CN104291500A (en) * | 2014-11-13 | 2015-01-21 | 北京赛科康仑环保科技有限公司 | Resourceful treatment system of low-concentration NH4Cl wastewater containing Mo and method of resourceful treatment system |
| CN109399850A (en) * | 2018-10-24 | 2019-03-01 | 科迈化工股份有限公司 | Rubber accelerator DPG waste water treatment process |
| CN109608252A (en) * | 2018-12-11 | 2019-04-12 | 中山市承铭农业技术开发有限公司 | A kind of production method of akaline liquid fertilizer |
| CN110921953A (en) * | 2019-12-06 | 2020-03-27 | 太原理工大学 | Resource treatment process and device for coking desulfurization waste liquid |
| CN113213518A (en) * | 2021-05-20 | 2021-08-06 | 安徽舜禹水务股份有限公司 | High ammonia nitrogen high alkalinity waste water resource system |
| CN114574530A (en) * | 2022-04-06 | 2022-06-03 | 齐齐哈尔龙江阜丰生物科技有限公司 | Method for recovering ammonium sulfate from glutamic acid mother liquor for L-lysine fermentation |
| CN116675396A (en) * | 2023-08-01 | 2023-09-01 | 成都瀚川环境科技有限公司 | Organic wastewater treatment system |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3029201A (en) * | 1959-12-28 | 1962-04-10 | Universal Oil Prod Co | Water treatment |
| EP0623554A1 (en) * | 1992-03-18 | 1994-11-09 | Uop | Treatment of an aqueous stream containing water-soluble inorganic sulfide compounds to selectively produce the corresponding sulfate |
| CN1121322A (en) * | 1993-12-28 | 1996-04-24 | 株式会社日本触媒 | Catalyst for processing waste water, production method thereof, and method of processing waste water using the catalyst |
| CN1365953A (en) * | 2002-02-01 | 2002-08-28 | 罗德春 | Integrated process for removing S, N and phenol from waste water containing S,N and phenol |
| CN101544381A (en) * | 2009-04-30 | 2009-09-30 | 江苏华达化工集团有限公司 | Method for producing ammonium sulphate by waste water produced in alpha naphthol production |
| CN101708870A (en) * | 2009-12-07 | 2010-05-19 | 江苏乐科热工程设备有限公司 | Concentration and crystallization process for ammonium sulphate waste liquor |
-
2010
- 2010-09-08 CN CN201010275155.8A patent/CN102398909B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3029201A (en) * | 1959-12-28 | 1962-04-10 | Universal Oil Prod Co | Water treatment |
| EP0623554A1 (en) * | 1992-03-18 | 1994-11-09 | Uop | Treatment of an aqueous stream containing water-soluble inorganic sulfide compounds to selectively produce the corresponding sulfate |
| CN1121322A (en) * | 1993-12-28 | 1996-04-24 | 株式会社日本触媒 | Catalyst for processing waste water, production method thereof, and method of processing waste water using the catalyst |
| CN1365953A (en) * | 2002-02-01 | 2002-08-28 | 罗德春 | Integrated process for removing S, N and phenol from waste water containing S,N and phenol |
| CN101544381A (en) * | 2009-04-30 | 2009-09-30 | 江苏华达化工集团有限公司 | Method for producing ammonium sulphate by waste water produced in alpha naphthol production |
| CN101708870A (en) * | 2009-12-07 | 2010-05-19 | 江苏乐科热工程设备有限公司 | Concentration and crystallization process for ammonium sulphate waste liquor |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103288286A (en) * | 2013-06-28 | 2013-09-11 | 陕西煤业化工技术研究院有限责任公司 | Catalytic oxidation treatment method for desulfurized waste liquid |
| CN103288286B (en) * | 2013-06-28 | 2015-03-18 | 陕西煤业化工技术研究院有限责任公司 | Catalytic oxidation treatment method for desulfurized waste liquid |
| CN104291500A (en) * | 2014-11-13 | 2015-01-21 | 北京赛科康仑环保科技有限公司 | Resourceful treatment system of low-concentration NH4Cl wastewater containing Mo and method of resourceful treatment system |
| CN104291500B (en) * | 2014-11-13 | 2016-04-13 | 北京赛科康仑环保科技有限公司 | A kind of lower concentration NH containing Mo 4the recycling treatment system of Cl waste water and method thereof |
| CN109399850A (en) * | 2018-10-24 | 2019-03-01 | 科迈化工股份有限公司 | Rubber accelerator DPG waste water treatment process |
| CN109608252A (en) * | 2018-12-11 | 2019-04-12 | 中山市承铭农业技术开发有限公司 | A kind of production method of akaline liquid fertilizer |
| CN110921953A (en) * | 2019-12-06 | 2020-03-27 | 太原理工大学 | Resource treatment process and device for coking desulfurization waste liquid |
| CN110921953B (en) * | 2019-12-06 | 2021-10-22 | 太原理工大学 | Resource treatment process and device for coking desulfurization waste liquid |
| CN113213518A (en) * | 2021-05-20 | 2021-08-06 | 安徽舜禹水务股份有限公司 | High ammonia nitrogen high alkalinity waste water resource system |
| CN114574530A (en) * | 2022-04-06 | 2022-06-03 | 齐齐哈尔龙江阜丰生物科技有限公司 | Method for recovering ammonium sulfate from glutamic acid mother liquor for L-lysine fermentation |
| CN116675396A (en) * | 2023-08-01 | 2023-09-01 | 成都瀚川环境科技有限公司 | Organic wastewater treatment system |
| CN116675396B (en) * | 2023-08-01 | 2023-11-10 | 成都瀚川环境科技有限公司 | Organic wastewater treatment system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102398909B (en) | 2014-11-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102398909B (en) | Method for producing ammonium sulfate by using high-ammonium-nitrogen sulfur-containing high-salinity wastewater | |
| Quan et al. | Simultaneous removal of ammonia, P and COD from anaerobically digested piggery wastewater using an integrated process of chemical precipitation and air stripping | |
| CN103693819B (en) | Thallium-containing heavy metal wastewater advanced treatment method | |
| CN102583847B (en) | Advanced treatment method of coking wastewater biochemical tail water | |
| CN105600990B (en) | Method for recycling sulfur, ammonium sulfate and catalyst by utilizing coke oven gas desulfurization and decyanation waste liquid | |
| CN110921953B (en) | Resource treatment process and device for coking desulfurization waste liquid | |
| CN101428933B (en) | Biological agent cooperated hydrolyzation-blowing off treatment process for nickel-ammonia wastewater | |
| CN102689977A (en) | Waste water purification method and reactor adopting ozone oxidation catalysis and using compound suspended carrier | |
| CN102976437A (en) | Method for treating arsenic in water with high-specific-surface-area Schwertmannite adsorbent | |
| CN105214599A (en) | Sulphur arsenic adsorbent and preparation method thereof | |
| CN106006681B (en) | A kind of method of high slat-containing wastewater recycling treatment | |
| CN100571849C (en) | A kind of treatment process of discharged doctor solution of HPF desulfurization system of coke-oven plant | |
| CN108947012B (en) | Method for separating and recovering ammonia from ammonia nitrogen wastewater | |
| CN113634587B (en) | Resource utilization method for desulfurization and sulfur by using magnesite | |
| CN102531274A (en) | Treatment method for ammonia nitrogen and COD (Chemical Oxygen Demand) in surface treatment waste water | |
| CN103145206B (en) | Composite nitrogen-removal medicament | |
| CN101428887B (en) | Treatment for nickel-ammonia wastewater with aeration-hydrolyzing process | |
| Ha et al. | Enhanced struvite (MgNH4PO4· 6H2O) granulation and separation from synthetic wastewater using fluidized-bed crystallization (FBC) technology | |
| JP4656848B2 (en) | Sludge treatment method | |
| CN105712570A (en) | Processing method of high concentration selenium-containing wastewater | |
| CN210764696U (en) | Reinforced up-flow type multiphase wastewater oxidation treatment system | |
| CN103523964A (en) | O&R (Ozone-Resin) harmless treatment process of cyanogens-containing tailing pulp | |
| CN111362507B (en) | Efficient chemical-biological degradation combined industrial wastewater treatment method | |
| CN207525037U (en) | One kind recycles high strength ammonia water system from ammonia nitrogen waste water | |
| CN102602994B (en) | Method for preparing arsenic trioxide by utilizing arsenious waste water |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| DD01 | Delivery of document by public notice |
Addressee: Fu Zeren Document name: Notification that Application Deemed not to be Proposed |
|
| ASS | Succession or assignment of patent right |
Owner name: BEIJING SAIKE KANGLUN ENVIRONMENTAL TECHNOLOGY CO. Free format text: FORMER OWNER: BEIJING SAIKE SHIDAI ENVIRONMENTAL TECHNOLOGY CO., LTD. Effective date: 20120601 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| COR | Change of bibliographic data |
Free format text: CORRECT: ADDRESS; FROM: 100080 HAIDIAN, BEIJING TO: 100085 HAIDIAN, BEIJING |
|
| TA01 | Transfer of patent application right |
Effective date of registration: 20120601 Address after: 100085, room 6, building 1, No. ten, 461 street, Beijing Applicant after: Beijing SaiKe Kanglun Environmental Science & Technology Co., Ltd. Address before: 100080, room 68, No. 909 West Fourth Ring Road, Haidian District, Beijing Applicant before: Beijing Saike Era Environmental Protection Technology Co.,Ltd. |
|
| 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: 100083 Beijing City, Haidian District Zhongguancun Road No. 18 smartfortune building block C room 1502 Applicant after: Beijing SaiKe Kanglun Environmental Science & Technology Co., Ltd. Address before: 100085, room 6, building 1, No. ten, 461 street, Beijing Applicant before: Beijing SaiKe Kanglun Environmental Science & Technology Co., Ltd. |
|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |