CN203501187U - Device for treating waste gas with high-concentration organic pollutants - Google Patents
Device for treating waste gas with high-concentration organic pollutants Download PDFInfo
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- CN203501187U CN203501187U CN201320482082.9U CN201320482082U CN203501187U CN 203501187 U CN203501187 U CN 203501187U CN 201320482082 U CN201320482082 U CN 201320482082U CN 203501187 U CN203501187 U CN 203501187U
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Abstract
The utility model provides a device for treating waste gas with high-concentration organic pollutants. The device is characterized by referring to a device with two integrated or split type combustion chambers which are improved from a combustion chamber of an integrated RTO (Regenerative Thermo Oxidation) device; meanwhile, high temperature waste gas in one of the two combustion chambers is led out; in combination with an external afterheat recycling device of the combustion chamber, the afterheat recycling utilization of surplus heat energy (overheat steam, saturated steam or hot water) of the second high temperature combustion chamber can be realized; if an ammonia gas supply device is additionally arranged for a waste gas entrance, the purification of NOx pollutants into N2 and H2O can also be realized, in combination with an SNCR (Selective Non-Catalytic Reduction) technology. According to the device, under the premise of keeping the advantages (high heat efficiency, high removal rate, low investment and small occupied area) of a traditional RTO technology, the technology limit that the traditional TRO technology only can be used for treating waste gas with low-concentration volatile organic pollutants is eliminated.
Description
Technical field
The utility model relates to a kind of device of processing waste gas, relate in particular to a kind of can be used in to process contain high concentration organic contaminant and NO
xthe device of the waste gas of pollutant.
Background technology
Along with the extensive use of Organic chemical products in industrial production, the volatile organic contaminant that enters into atmosphere is more and more.The discharge of these pollutants not only severe contamination environment, the deep life and health that has jeopardized tellurian also.At present, the removal method of volatile organic contaminant or technique mainly comprise several different methods or the techniques such as bioanalysis, combustion method, low temperature plasma decomposition method, wherein combustion method technique be at present the most ripe, pollutant removal is the most thorough and most widely used technology.
The principle of combustion method technique is at high temperature to make volatile organic contaminant waste gas and fuel gas fully mixed, realize completing combustion, volatile organic contaminant waste gas is oxidized to the harmless carbon dioxide of odorless and water, combustion method technique mainly can be divided into flame combustion method (TO, Thermo Oxidation) technique, catalytic combustion (CO, Catalytic Oxidation) method technique, heat storage type combustion method (RTO, Regenerative Thermo Oxidation) technique are three kinds.
Flame combustion method technique, is that the high-temperature fuel gas that auxiliary fuel burning is produced fully mixes with volatile organic contaminant waste gas, makes volatile organic contaminant waste gas at 700～900 ℃, be oxidized destruction.While using this method to process waste gas, guarantee that waste gas is by complete oxidation, partial oxidation likely increases stink, and for example ethanol incomplete oxidation may change carboxylic acid into.The advantage of flame combustion method is that removal is thorough, efficiency is high, but needs to supplement enough fuel, and in the time of especially will obtaining more than 99.9% purifying rate, ignition temperature need be greater than 872 ℃, even will reach 982 ℃.Secondly, if while containing the elements such as S, N, Cl in organic exhaust gas composition, the product after burning has the nuisances such as sulfur oxide (sulfur dioxide, sulfur trioxide), nitrogen oxide, hydrogen chloride, free chlorine, must process in conjunction with processes such as absorption or absorption, to avoid secondary pollution.
Catalytic oxidation technique refers under catalyst action, and volatile organic contaminant waste gas is (300-600 ℃) lower oxidation reaction that occurs at a lower temperature, generates carbon dioxide and water, to reach the object of removing organic pollution.The advantages such as compare with flame combustion method technique, it is low that Production by Catalytic Combustion Process technique has oxidizing temperature, and device volume is little, and its material and thermal expansion problem easily solve, disposal cost is low.The efficiency of catalytic combustion can reach more than 90%, and disposal cost is only half left and right of flame combustion method technique.The feature of this technology maximum is exactly nonflame, and initiation temperature is low, has greatly suppressed airborne N
2oxidation forms NO
x.Due to the low temperature nonstaining property of Production by Catalytic Combustion Process technique, and relatively low with respect to high temperature incineration technological investment, in recent years, in petrochemical industry VOCs treatment, progressively obtained more utilization.But general the organic compound for particular type of catalyst in this technique, and in volatile organic contaminant waste gas, often there is impurity, be easy to cause catalyst poisoning.Because pollutant kind is many, complicated components, content is low, will focus on the selection of catalyst during design, guarantees high purification efficiency.
Heat-accumulation combustion method technique refers to that a volatile organic contaminant waste gas is heated to more than 760 ℃, makes the volatile organic contaminant oxidation Decomposition in waste gas become carbon dioxide and water.The high-temperature gas that oxidation the produces special heat storage of flowing through, heats up and " accumulation of heat " heat storage, and this " accumulation of heat " for the follow-up volatile organic contaminant waste gas entering of preheating, thereby saves the fuel consumption that waste gas heats up.With other oxidative system comparison, RTO technique has better recuperation of heat utility, greatly reduces the operating cost of processing procedure, and device is compact, and plant investment is minimum.
RTO technique can be by single, two regenerator or three regenerator or five or seven regenerator and an integrated RTO device waste gas cleaning system that combustion chamber forms.The RTO technique of three symmetrical regenerator and a combustion chamber of now take is introduced as example, and its operation principle is shown in Fig. 1.Volatile organic contaminant waste gas 1 is introduced into ceramic heat-storing chamber 5 under air blast 2 effects, enters combustion chamber 3 after heat absorption, guarantees that chamber temperature is at 760 ℃-850 ℃, thereby guarantees high clearance and toxic emission compliance rate.
The feature performance benefit of RTO technique:
(1) purification efficiency is high, more than two Room can reach 94%-99%.
(2) heat recovery efficiency high (>90%), energy-conservation, in organic exhaust gas, more than the concentration 2g/Nm3 of organic pollution can reach thermal balance, without the outer heat energy of giving.
(3) resistance low (being generally less than 5kPa), system installed power is little, energy-conservation and operating cost is lower.
(4) device can high temperature resistant (～1000 ℃), and normal temperature is 760 ℃-850 ℃.
At present, RTO technology is more and more ripe, at the environmental protection industry (epi) of China, has also obtained application more and more widely, and, RTO technology mainly in, low concentration (<2.0g/Nm
3) purification of volatile organic contaminant waste gas, but in the production process of most petroleum and petrochemical industry or other chemical plant installations, produce and in actual waste gas, contain often a large amount of high concentration (>2g/Nm
3) volatile organic contaminant or also with a certain amount of nitrogen oxide (NO
x) mix waste gas, for this high concentration (>2g/Nm
3) organic pollution waste gas, especially also contain nitrogen oxide (NO
x) exhaust-gas treatment, traditional RTO technique inapplicable.
Utility model content
This practicality is newly to be solved is that current RTO technique can not be applicable to contain high concentration (>2g/Nm
3) organic pollution waste gas, especially also contain nitrogen oxide (NO
x) the problem of processing of waste gas.
To achieve these goals, the utility model provides the device that a kind of processing contains high concentration organic contaminant waste gas.
The device that a kind of processing that the utility model provides contains high concentration organic contaminant waste gas, comprise: combustion chamber, pending waste gas pipeline road, ammonia conveyance conduit, three regenerator, wherein, three regenerator are connected in parallel on pending waste gas pipeline road, and all communicate with combustion chamber; Between pending waste gas pipeline road and regenerator, be respectively arranged with valve; Described regenerator is respectively equipped with fluid expulsion pipeline, and the fluid expulsion pipeline of regenerator is communicated with chimney, and fluid expulsion pipeline is provided with valve.
Wherein, described combustion chamber comprises the first chamber and the second chamber communicating, and wherein, the first chamber connects auxiliary fuel interface, and storage heater is communicated with the first chamber; The second chamber is provided with fluid expulsion pipeline, and the fluid expulsion pipeline of the second chamber is communicated with chimney after by residual neat recovering system.
Wherein, ammonia conveyance conduit, is communicated with storage heater.And preferably, ammonia conveyance conduit was merged into same pipeline with pending waste gas pipeline road before being communicated with storage heater.
Preferably, the connected entrance between the first chamber and the second chamber is positioned at the one end away from auxiliary fuel interface.
Preferably, the connected entrance between the first chamber and the second chamber is positioned at the one end away from the fluid expulsion pipeline of the second chamber.
In a kind of preferred embodiment of the present utility model, also comprise back blowing machine, the fluid expulsion pipeline of the second chamber and/or regenerator fluid expulsion pipeline are communicated with respectively back blowing machine air inlet, and back blowing machine air outlet is communicated with described storage heater.
Wherein, the fluid expulsion pipeline of the second chamber and/or regenerator fluid expulsion pipeline can be respectively by being communicated with back blowing machine air inlet after chimney independently, and/or before being communicated with chimney, by lateral, are communicated with reverse hair-dryer.
Preferably, between back blowing machine air outlet and storage heater, valve is set.
Preferably, the fluid expulsion pipeline of the second chamber is communicated with back blowing machine air inlet after by residual neat recovering system.
In a kind of preferred embodiment of the present utility model, described combustion chamber is designed for integral type, and in combustion chamber, dividing plate is set, and combustion chamber is divided into the first chamber and the second chamber.
Described residual neat recovering system can be can carry out the device of heat exchange arbitrarily, and more preferably, described residual neat recovering system can also carry out store heat simultaneously.
Such as, described residual neat recovering system can be the independent regenerator arranging, heat exchanger, phase transformation storage device etc.
In a kind of preferred embodiment of the present utility model, the fluid expulsion pipeline of the second chamber is also provided with the second lateral, and the second lateral was communicated with back blowing machine air inlet before residual neat recovering system.
Should be understood that the optional preferred embodiment that the present embodiment is above-mentioned, any unrestricted combination mutually.
The device of processing waste gas provided by the utility model, take traditional RTO device as basis, a high temperature combustors of integrated RTO device (760 ℃-850 ℃) is improved to the device of two integrated or split type high temperature combustors (760 ℃-1200 ℃), can realizes from the waste heat recovery (recyclable superheated steam, saturated vapor or hot water) of high temperature purification gas in high-temperature burner hearth and utilizing.Retain traditional RTO technology advantage (thermal efficiency is high, clearance is high, reduced investment and floor space little) prerequisite under, solved traditional RTO technique and only can process the process limitations of light-concentration volatile organic pollution waste gas.
In conjunction with SNCR (SNCR, Selective Non-Catalytic Reduction) technology, the utility model can improve combustion chamber interior reaction temperature to 930 ℃～1200 ℃, sets up ammonia induction system simultaneously, when can realize organic pollution VOC and NOx pollutant, purifies.Can process high concentration (>2g/Nm
3) volatile organic contaminant or also with a certain amount of nitrogen oxide (NO
x) mix waste gas, the technology that has made up traditional RTO technique is limited to.
Processing described in the utility model is containing the device of high density pollution thing waste gas, main application fields comprises the improvement of the waste gas such as petroleum and petrochemical industry, metallurgy, chemical fertilizer, light industry, surface spraying, as the waste gas containing organic pollution and NOx, acrylonitrile off-gas, acrylic acid tail gas, phthalic anhydride, cis-butenedioic anhydride, maleic acid tail gas, styrene tail gas, phenol-acetone tail gas, polyacrylamide tail gas, ABS tail gas, butadiene-styrene rubber, butadiene rubber, butyl rubber tail gas, sewage treatment plant's foul waste gas etc.
Accompanying drawing explanation
Fig. 1 is traditional RTO process flow diagram;
Fig. 2 is treating apparatus process flow diagram in a kind of embodiment of the utility model;
Fig. 3 is treating apparatus process flow diagram in the another kind of embodiment of the utility model.
The specific embodiment
With reference to Fig. 2, in a kind of embodiment of the utility model, the device that processing contains high density pollution thing as shown in Figure 2, comprises combustion chamber 12, is provided with dividing plate 123 and combustion chamber 12 is separated into the first chamber 121 and the second chamber 122 being communicated with at right-hand member in the middle of combustion chamber 12.
The first chamber 121 is communicated with three regenerator 11, is respectively the first regenerator 11A, the second regenerator 11B and the 3rd regenerator 11C.Three regenerator 11 are connected in parallel on pending waste gas pipeline road 100.
The first chamber 121 left sides are provided with auxiliary fuel import 42, for the 12 interior infeed auxiliary fuels to combustion chamber; The second chamber 122 left sides connect gas outlet pipe road 130, for the gaseous product after burning is discharged by chimney 50.
The gas outlet pipe road 130 of the second chamber is before entering chimney 50, by residual neat recovering system 13(such as phase change material device or simple heat exchanger etc., or the independent regenerator arranging), in residual neat recovering system 13, carry out heat exchange, the gas storage that the heat that burning is produced passes through to discharge is in waste heat stocking system 13.
Embodiment 1
Pending waste gas 10, ammonia 20 and air 30 are all communicated to pending waste gas pipeline road 100, and send in the first storage heater 11A.
The first storage heater 11A is heated to 850-900 ℃ in advance, the ceramic bed of having accumulated heat in the first storage heater 11A make through gas preheating (ceramic heat-storing bed is cooling), the waste gas after being preheated is sent into the first chamber 121 of combustion chamber 12.
Meanwhile, auxiliary fuel is sent in the first chamber 121 by the auxiliary fuel entrance 42 in left side, and combustion fan 41 is blown into oxygen or air auxiliary combustion in the first chamber 42 simultaneously.The right-hand member of gas by the first chamber 121 enters the second chamber 122 and burns away.Fully reaction under the interior hot conditions in combustion chamber 12, and emit a large amount of heat, make chamber temperature rise to 1050 ℃-1100 ℃, in combustion chamber 12, organic pollution is decomposed and destroys, meanwhile, NO
xby ammonia, be reduced to N
2and water.
High-temperature gas after partial combustion is sent into the second regenerator 11B, by heat exchange, the second regenerator is heated, then by fluid expulsion pipeline 110, send into chimney 50 and discharge (especially in the situation of sufficient combustion), or sending into back blowing machine 60(especially burns in inadequate situation), by 60 couples of the 3rd regenerator 11C of back blowing machine, carry out blowback and go back to combustion chamber.
After 10s-2min, close the air intake valve of the first regenerator 11A, pending waste gas changes by the second regenerator 11B and enters combustion chamber 12, and carries out preheating by the second regenerator 11B.Now, the high-temperature gas after partial combustion is sent into the 3rd regenerator 11C, and the 3rd regenerator is heated, and back blowing machine 60 returns the blow-back of discharge to the first regenerator 11A simultaneously.
After 10s-2min, close the air intake valve of the second regenerator 11B, pending waste gas changes by the 3rd regenerator 11C and enters combustion chamber 12, and carries out preheating by the 3rd regenerator 11C.High-temperature gas after partial combustion is sent into the first regenerator 11A, and the first regenerator is heated, and back blowing machine 60 returns the blow-back of discharge to the second regenerator 11B simultaneously.
Iterative cycles said process, until pending exhaust-gas treatment is complete, waste gas is constantly circulation between three regenerator, and one of them regenerator is the heating by the exhaust gases entering, be the ceramic dielectric heat of waste-gas heat after raw material waste gas is processed by " absorption is accumulated ", self obtain preheating or discharge heat energy; A regenerator is cooling for the purified gas of discharging, and ceramic bed is heated; A regenerator is swept state in blowback, and the blow-back after residual untreated organic exhaust gas is cleaned goes back to combustion chamber and carries out incineration process.Therefore, each regenerator ceramic bed can experience one " cooling →. purify →. heating " cyclic process.The heat that utilizes burning to produce like this carries out preheating to pending waste gas, guarantees that ignition temperature is at 1050-1100 ℃.
In combustion chamber, the 12 interior time of staying were designed to > 1.5s to pending gas, to guarantee sufficient reacting.Waste gas is exported by the second gas outlet, upper furnace left side, gas outlet pipe road 130 is through pre-heat recovery system 13, by remaining heat absorption, wherein, part waste gas directly enters chimney 60 and discharges, another part waste gas after branch pipe(tube) 131 and blender 61 mixing, enters blowback purging system by back blowing machine 60 after passing through residual neat recovering system 13.
The second branch pipe(tube) 132, after blender 61 mixes, enters blowback purging system by back blowing machine 60.Like this, after pending exhaust-gas treatment, the processed waste gas that can send by another gas outlet pipe road 132 of the second chamber 122 carries out blowback to whole system, thereby guarantees not have waste gas residual.
Embodiment 2
With reference to Fig. 3, with reference to embodiment 1, in the present embodiment, combustion chamber 12 comprises that 122 of the first chamber 121 and the second chamber 122, the second chambers are as a regenerator independently.Waste gas after burning delivers into two gas outlet pipe roads by the second chamber below, a gas outlet pipe road 130 wherein, gas outlet pipe road 130 is through pre-heat recovery system 13, by remaining heat absorption, wherein, part waste gas directly enters chimney 60 and discharges, and another part waste gas after branch pipe(tube) 131 and blender 61 mixing, enters blowback purging system by back blowing machine 60 after passing through residual neat recovering system 13.Another gas outlet pipe road (the second branch pipe(tube)) 132, after blender 61 mixes, enters blowback purging system by back blowing machine 60.
Above specific embodiment of the utility model be have been described in detail, but it is just as example, the utility model is not restricted to specific embodiment described above.To those skilled in the art, any equivalent modifications that the utility model is carried out and alternative also all among category of the present utility model.Therefore,, not departing from the equalization conversion of doing under spirit and scope of the present utility model and revising, all should be encompassed in scope of the present utility model.
Claims (8)
1. the device that processing contains high concentration organic contaminant waste gas, it is characterized in that, described device comprises: combustion chamber, pending waste gas pipeline road, ammonia conveyance conduit, three regenerator, wherein, three regenerator are connected in parallel on pending waste gas pipeline road, and all communicate with combustion chamber; Between pending waste gas pipeline road and regenerator, be respectively arranged with valve; Described regenerator is respectively equipped with fluid expulsion pipeline, and the fluid expulsion pipeline of regenerator is communicated with chimney, and fluid expulsion pipeline is provided with valve; And ammonia conveyance conduit, is communicated with storage heater;
Wherein, described combustion chamber comprises the first chamber and the second chamber communicating, and wherein, the first chamber connects auxiliary fuel interface, and storage heater is communicated with the first chamber; The second chamber is provided with fluid expulsion pipeline, and the fluid expulsion pipeline of the second chamber is communicated with chimney after by residual neat recovering system.
2. device according to claim 1, is characterized in that, ammonia conveyance conduit was merged into same pipeline with pending waste gas pipeline road before being communicated with storage heater.
3. device according to claim 1, is characterized in that, also comprises back blowing machine, and the fluid expulsion pipeline of the second chamber and/or regenerator fluid expulsion pipeline are communicated with respectively back blowing machine air inlet, and back blowing machine air outlet is communicated with described storage heater.
4. device according to claim 1, is characterized in that, described combustion chamber is designed for integral type, and in combustion chamber, dividing plate is set, and combustion chamber is divided into the first chamber and the second chamber.
5. device according to claim 1, is characterized in that, the fluid expulsion pipeline of the second chamber is communicated with back blowing machine air inlet after by residual neat recovering system.
6. device according to claim 1, is characterized in that, the fluid expulsion pipeline of the second chamber is also provided with lateral, and lateral was communicated with back blowing machine air inlet before residual neat recovering system.
7. device according to claim 1, is characterized in that, the connected entrance between the first chamber and the second chamber is positioned at the one end away from auxiliary fuel interface.
8. device according to claim 1, is characterized in that, the connected entrance between the first chamber and the second chamber is positioned at the one end away from the fluid expulsion pipeline of the second chamber.
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|---|---|---|---|
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104110688A (en) * | 2014-07-08 | 2014-10-22 | 安徽福斯特汽车部件有限公司 | Water heating furnace utilizing waste gas incineration |
| CN104344409A (en) * | 2013-08-07 | 2015-02-11 | 上海同济华康环境科技有限公司 | Method for processing exhaust gas containing high-concentration organic pollutant |
| CN104534487A (en) * | 2014-12-16 | 2015-04-22 | 江苏百茂源环保科技有限公司 | Heat storage burning system |
| CN106705076A (en) * | 2016-12-30 | 2017-05-24 | 天津燃洁斯工业设备有限公司 | Heat storage incineration furnace |
| CN106731562A (en) * | 2015-11-19 | 2017-05-31 | 中国石油化工股份有限公司 | A kind of integrated conduct method and device of the chloride organic exhaust gas of high concentration |
| CN108373233A (en) * | 2018-01-25 | 2018-08-07 | 浙江奇彩环境科技股份有限公司 | A kind of processing method of organic amine wastewater |
| CN108744869A (en) * | 2018-05-28 | 2018-11-06 | 浙江大学 | A kind of molecular sieve purification devices and methods therefor using twin-stage heat pipe phase change heat accumulator |
| CN111842457A (en) * | 2020-06-24 | 2020-10-30 | 永清环保股份有限公司 | Ectopic thermal desorption method and device for oil sludge or organic contaminated soil |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104344409A (en) * | 2013-08-07 | 2015-02-11 | 上海同济华康环境科技有限公司 | Method for processing exhaust gas containing high-concentration organic pollutant |
| CN104110688B (en) * | 2014-07-08 | 2016-08-31 | 安徽福斯特汽车部件有限公司 | Burned waste gas water heater |
| CN104110688A (en) * | 2014-07-08 | 2014-10-22 | 安徽福斯特汽车部件有限公司 | Water heating furnace utilizing waste gas incineration |
| CN104534487A (en) * | 2014-12-16 | 2015-04-22 | 江苏百茂源环保科技有限公司 | Heat storage burning system |
| CN106731562B (en) * | 2015-11-19 | 2019-08-06 | 中国石油化工股份有限公司 | A kind of integrated conduct method and device of high concentration organic exhaust gas containing chlorine |
| CN106731562A (en) * | 2015-11-19 | 2017-05-31 | 中国石油化工股份有限公司 | A kind of integrated conduct method and device of the chloride organic exhaust gas of high concentration |
| CN106705076B (en) * | 2016-12-30 | 2019-10-18 | 天津燃洁斯工业设备有限公司 | Thermal accumulating incinerator |
| CN106705076A (en) * | 2016-12-30 | 2017-05-24 | 天津燃洁斯工业设备有限公司 | Heat storage incineration furnace |
| CN108373233A (en) * | 2018-01-25 | 2018-08-07 | 浙江奇彩环境科技股份有限公司 | A kind of processing method of organic amine wastewater |
| CN108744869A (en) * | 2018-05-28 | 2018-11-06 | 浙江大学 | A kind of molecular sieve purification devices and methods therefor using twin-stage heat pipe phase change heat accumulator |
| CN108744869B (en) * | 2018-05-28 | 2020-08-11 | 浙江大学 | Molecular sieve purifying device and method utilizing two-stage heat pipe phase-change heat accumulator |
| CN111842457A (en) * | 2020-06-24 | 2020-10-30 | 永清环保股份有限公司 | Ectopic thermal desorption method and device for oil sludge or organic contaminated soil |
| CN111842457B (en) * | 2020-06-24 | 2022-04-08 | 永清环保股份有限公司 | Ectopic thermal desorption method and device for organic contaminated soil |
| CN112864408A (en) * | 2020-12-23 | 2021-05-28 | 周宗霞 | Equipment for removing and recycling mercury for waste battery |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: XINJIANG TONGJI ECOLOGICAL TECHNOLOGY CO., LTD. Effective date: 20150716 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20150716 Address after: 200092, room 3, floor 557, No. 8357 West Dalian Road, Shanghai, Hongkou District Patentee after: Tongji Huakang Environment Science and Technology Co., Ltd., Shanghai Patentee after: Xinjiang Tongji eco Polytron Technologies Inc Address before: 200092, room 3, floor 557, No. 8357 West Dalian Road, Shanghai, Hongkou District Patentee before: Tongji Huakang Environment Science and Technology Co., Ltd., Shanghai |
|
| CU03 | Correction of utility model patent gazette |
Correction item: Patentee|Address|Patentee Correct: Tongji Huakang Environment Science and Technology Co., Ltd., Shanghai|200092, room 3, floor 557, No. 8357 West Dalian Road, Shanghai, Hongkou District|XJTJ Ecological Technology Engineering Co., Ltd. False: Tongji Huakang Environment Science and Technology Co., Ltd., Shanghai|200092, room 3, floor 557, No. 8357 West Dalian Road, Shanghai, Hongkou District|Xinjiang Tongji eco Polytron Technologies Inc Number: 31 Volume: 31 |
|
| ERR | Gazette correction | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20140326 Termination date: 20150807 |
|
| EXPY | Termination of patent right or utility model |