CN102247752A - Flue gas treatment system of tank furnace and flue gas treatment method thereof - Google Patents
Flue gas treatment system of tank furnace and flue gas treatment method thereof Download PDFInfo
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- CN102247752A CN102247752A CN2011102015277A CN201110201527A CN102247752A CN 102247752 A CN102247752 A CN 102247752A CN 2011102015277 A CN2011102015277 A CN 2011102015277A CN 201110201527 A CN201110201527 A CN 201110201527A CN 102247752 A CN102247752 A CN 102247752A
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Abstract
The invention relates to a flue gas treatment system of a tank furnace, which comprises a denitration system, a deboration system and a flue gas exhaust system, wherein the denitration system comprises an SNCR (Selective Non-Catalytic Reduction) denitration segment, a carbamide solution storage tank and a metering pump; the deboration system comprises a spray cooling tower, a first circulating pool, a first circulating pump, an absorption reaction tower, a second circulating pool, a second circulating pump, an alkali liquor preparation tank, an alkali liquor supply pump, an efflux pump and a centrifugal machine; and the flue gas exhaust system comprises an electric heater, an air blower and a chimney. The invention also relates to a flue gas treatment method of the flue gas treatment system of the tank furnace, comprising the following steps of: firstly removing NO contained in flue gas; then carrying out deboration treatment on the flue gas with NO removed; and finally exhausting the flue gas subjected to the deboration treatment. According to the flue gas treatment system and the flue gas treatment method thereof disclosed by the invention, borides and nitrogen oxides which are contained in the flue gas can be effectively treated, and the material dust condensation blocking and the boride blocking of a flue are effectively prevented from being generated.
Description
Technical field
The present invention relates to the flue gas process field, relate in particular to system and flue gas processing method thereof that a kind of TFT-LCD base plate glass tank furnace gas is handled.
Background technology
At present, boride in the TFT-LCD base plate glass tank furnace gas (5g/Nm3), nitrogen oxide (9.6g/Nm3) content are higher, easily to producing and atmospheric environment impacts.Except that high temperature sodium salt material dirt and half-cooked material easily cause condense stop up, boride also results in blockage to flue easily, thereby influence that flue gas is discharged and the stablizing of furnace pressure; Tank furnace adopts pure oxygen burning, and oxygen is excessive, and nitric oxide partly is converted into nitrogen dioxide, also can cause very big corrosiveness to equipment.All adopt the dry process mode at present at the TFT-LCD base plate glass tank furnace gas in the prior art.This processing mode can not effectively be controlled the condensation problem of boride, nitrogen oxide and sodium salt material dirt and half-cooked material in the flue gas.
Summary of the invention
The tank furnace smoke processing system and the flue gas processing method thereof that condense and stop up that the object of the present invention is to provide boride and the nitrogen oxide in a kind of effectively smoke treatment and control sodium salt material dirt.
For achieving the above object, the present invention is by the following technical solutions: a kind of tank furnace smoke processing system, it comprises denitrating system, takes off boron system and flue gas emission, described denitrating system comprises SNCR denitration section, the urea liquid storage tank and the measuring pump that are connected with SNCR denitration section, and wherein SNCR denitration section is arranged on the tank furnace exhanst gas outlet pipeline; The described boron system of taking off comprises water cooling tower, first circulatory pool, first circulating pump, absorption reaction tower, second circulatory pool, second circulating pump, alkali lye preparing tank, alkali lye supply pump, efflux pump and centrifuge, wherein water cooling tower is connected with SNCR denitration section by flue, first circulatory pool is connected with the bottom of water cooling tower by fluid pipeline, first circulating pump is connected with first circulatory pool by fluid pipeline, and this first circulating pump is connected to the top of water cooling tower by fluid pipeline; The bottom of absorption reaction tower is connected with the water cooling tower top by flue, second circulatory pool is connected by the bottom of fluid pipeline with the absorption reaction tower, second circulating pump is connected with second circulatory pool by fluid pipeline, and this second circulating pump is connected to the top of absorption reaction tower by fluid pipeline, the alkali lye preparing tank is connected with the alkali lye supply pump by fluid pipeline, and the alkali lye supply pump is connected with second circulatory pool by fluid pipeline; Efflux pump is connected with second circulatory pool by fluid pipeline, and this efflux pump is connected with centrifuge by fluid pipeline; Described flue gas emission comprises electric heater, blower fan and chimney, and wherein electric heater is connected by the top of flue with the absorption reaction tower, and blower fan is connected with electric heater by flue, and chimney is connected with the blowing mouth of blower fan.
Further, described second circulatory pool is connected with first circulating pump by fluid pipeline, and wherein fluid pipeline is provided with by-pass valve control.
Further, this tank furnace smoke processing system also comprises by-pass flue, and an end of this by-pass flue is connected the outlet of SNCR denitration section, and the other end of this by-pass flue is connected the outlet of electric heater.
Further, the top exit of described absorption reaction tower is provided with demister.
Further, the flue before the described SNCR denitration section is provided with heat-insulation layer; Flue between described SNCR denitration section and the water cooling tower is provided with heat-insulation layer equally.
The present invention also provides a kind of flue gas processing method of tank furnace smoke processing system, and described method is carried out according to following steps:
Step 1: remove the NO gas in the flue gas: 850 ℃-1100 ℃ tank furnace flue gas enters SNCR denitration section, and measuring pump sprays into SNCR denitration section with the urea liquid of urea liquid storage tank, and the NO gas in urea and the flue gas reacts, and generates the nitrogen G﹠W;
Step 2: to removing NO
xFlue gas takes off boron to be handled:
At first, flue gas enters water cooling tower, spray cooling solution in first circulatory pool is delivered to water cooling tower top by first circulating pump, flue gas is carried out damping cooling and the most of washing of boron compound is entered in the spray solution by the spray cooling solution, be disposed in first circulatory pool, the spray cooling solution is constantly circulation between first circulatory pool and water cooling tower again; Wherein flue gas enters the water cooling tower inlet temperature more than 500 ℃, and flue gas is discharged the water cooling tower outlet temperature at 55-70 ℃, and the control liquid-gas ratio is 5-10L/Nm3; The spray cooling solution is constantly circulation between first circulatory pool and water cooling tower, waits to spray when institute's boron-containing compound reaches finite concentration in the cooling solution entering in second circulatory pool by first circulating pump;
Subsequently, flue gas is discharged again from the top that sprays cooling tower, and the bottom of self-absorption reaction tower enters the absorption reaction tower, sodium hydroxide solution in the alkali lye preparing tank is delivered in second circulatory pool by the alkali lye supply pump, be delivered to the top of absorption reaction tower again by second circulating pump, contact with flue gas adverse current at the absorption reaction tower, sodium hydroxide solution with flow back in second circulatory pool after flue gas contacts, control sodium hydroxide solution pH＜9.6, making the product in second circulatory pool is borax, when the borax soln in second circulatory pool reaches finite concentration, drain into centrifuge by efflux pump and carry out centrifugally, isolate the solid borax, liquid is back to second circulatory pool;
Step 3: to discharging through taking off the flue gas that boron handles: the demister at the top through taking off the flue gas self-absorption reaction tower that boron handles is expelled to electric heater, and flue gas improves through the electric heater temperature after blower fan, smoke stack emission.
Wherein, the chemical equation of the chemical reaction that takes place in second circulatory pool in the described step 2 is:
4H
3BO
3+2NaOH＝Na
2[B
4O
5(OH)
4]+5H
2O。
Wherein, be added with oxidant in the sodium hydroxide solution of described absorption reaction tower, this oxidant is converted into nitrogen dioxide with part nitric oxide in the flue gas.
Wherein, the injection flow rate of described water cooling tower control liquid-gas ratio is 5-10L/Nm
3, the exhanst gas outlet temperature is controlled at 55-70 ℃.
Adopt tank furnace smoke processing system of the present invention and processing method thereof, can reach more than 80%, can reach more than 98% the boride disposal ability to the disposal ability of nitrogen oxide.In the entire process process, cooling water can carry out 100% and recycle, and except that required firm power, does not need extra energy supply substantially, has effectively saved the cost that flue gas is handled.
The surface temperature of the present invention by exhaust gases passes before the control control water cooling tower and equipment is more than 500 ℃, and the surface temperature of the exhaust gases passes before the SNCR denitration section is more than 800 ℃, and control is 8-11m/s with the flue gas flow rate in the upper flue.Can effectively prevent the obstruction of condensing of sodium salt material dirt and half-cooked material like this.
Except that blower motor, circulating pump motor, not having to provide needs extra kinetic energy and does not produce noxious pollutant in the entire process process of the present invention.Smoke exhaust fan outlet flue gas cleaning, TSP, PM10 are all up to standard.Advantage such as that the present invention has is simple, stable, the flue gas treatment effect is obvious.
Description of drawings
Fig. 1 is the structural representation of tank furnace smoke processing system according to the invention.
The present invention will be further described below in conjunction with the drawings and specific embodiments.
The specific embodiment
Please refer to Fig. 1, the tank furnace smoke processing system comprises denitrating system, takes off boron system and flue gas emission.
Described denitrating system comprises SNCR denitration section 1, the urea liquid storage tank 2 and the measuring pump 3 that are connected with SNCR denitration section 1, and wherein SNCR denitration section 1 is arranged on the tank furnace exhanst gas outlet pipeline.Flue before the wherein said SNCR denitration section 1 is provided with heat-insulation layer (not shown).
The described boron system of taking off comprises water cooling tower 4, first circulatory pool 5, first circulating pump 6, absorption reaction tower 7, second circulatory pool 8, second circulating pump 9, alkali lye preparing tank 10, alkali lye supply pump 11, efflux pump 12 and centrifuge 13.
Wherein water cooling tower 4 is connected with SNCR denitration section 1 by flue.First circulatory pool 5 is connected by the bottom of fluid pipeline with water cooling tower 4.First circulating pump 6 is connected with first circulatory pool 5 by fluid pipeline, and this first circulating pump 6 is connected to the top of water cooling tower 4 by fluid pipeline.Flue between described water cooling tower 4 and the SNCR denitration section 1 is provided with heat-insulation layer (not shown) equally.
The bottom of absorption reaction tower 7 is connected with water cooling tower 4 tops by flue.Second circulatory pool 8 is connected by the bottom of fluid pipeline with absorption reaction tower 7.Described second circulatory pool 8 also is connected with first circulating pump 6 by fluid pipeline, and wherein fluid pipeline is provided with by-pass valve control.Second circulating pump 9 is connected with second circulatory pool 8 by fluid pipeline, and this second circulating pump 9 is connected to the top of absorption reaction tower 7 by fluid pipeline.Alkali lye preparing tank 10 is connected with alkali lye supply pump 11 by fluid pipeline, and alkali lye supply pump 11 is connected with second circulatory pool 8 by fluid pipeline.
Efflux pump 12 is connected with second circulatory pool 8 by fluid pipeline, and this efflux pump 11 is connected with centrifuge 13 by fluid pipeline.
The top exit of described absorption reaction tower 7 is provided with demister 17.
Described flue gas emission comprises electric heater 14, blower fan 15 and chimney 16, wherein electric heater 14 is connected by the top of flue with absorption reaction tower 7, blower fan 15 is connected with electric heater 14 by flue, and chimney 16 is connected with the blowing mouth of blower fan 15.
This tank furnace smoke processing system also comprises by-pass flue 18, and an end of this by-pass flue 18 is connected the outlet of SNCR denitration section 1, and the other end of this by-pass flue 18 is connected the outlet of electric heater 14.By-pass flue 18 is provided with by-pass valve control.
The flue gas processing method of described tank furnace smoke processing system, carry out according to following steps:
Step 1: remove the NO in the flue gas
x: 850 ℃-1100 ℃ tank furnace flue gas enters SNCR denitration section 1, and measuring pump 3 sprays into SNCR denitration section 1, the NO in urea and the flue gas with the urea liquid of urea liquid storage tank 2
xReact, generate the nitrogen G﹠W.Wherein said flue gas enters the surface temperature of the flue before the SNCR denitration section more than 800 ℃, and flue gas flow rate is 8-11m/s.
Step 2: to removing NO
xFlue gas takes off boron to be handled:
At first, flue gas enters water cooling tower 4, spray cooling solution in first circulatory pool 5 is delivered to water cooling tower 4 tops by first circulating pump 6, flue gas is carried out damping cooling and the most of washing of boron compound is entered in the spray solution by the spray cooling solution, be disposed in first circulatory pool 5, the spray cooling solution is constantly circulation between first circulatory pool 5 and water cooling tower 4 again; Wherein flue gas enters water cooling tower 1 inlet temperature more than 500 ℃, and flue gas is discharged water cooling tower 1 outlet temperature at 55-70 ℃, and the control liquid-gas ratio is 5-10L/Nm3; Wait to spray when institute's boron-containing compound reaches finite concentration in the cooling solution and enter in second circulatory pool 8 by first circulating pump 6.Wherein said flue gas enters the surface temperature of water cooling tower (4) flue before more than 500 ℃, and flue gas flow rate is 8-11m/s.
Subsequently, flue gas is discharged again from the top that sprays cooling tower 4, and the bottom of self-absorption reaction tower 7 enters absorption reaction tower 7, sodium hydroxide solution in the alkali lye preparing tank 10 is delivered in second circulatory pool 8 by alkali lye supply pump 11, be delivered to the top of absorption reaction tower 7 again by second circulating pump 9, contact with flue gas adverse current at absorption reaction tower 7, sodium hydroxide solution with flow back in second circulatory pool 8 after flue gas contacts, control sodium hydroxide solution pH＜9.6, making the product in second circulatory pool 8 is borax, when the borax soln in second circulatory pool 8 reaches finite concentration, draining into centrifuge 13 by efflux pump 12 carries out centrifugal, isolate the solid borax, liquid is back to second circulatory pool 8.The chemical equation of the chemical reaction that takes place in second circulatory pool 8 is:
4H
3BO
3+2NaOH＝Na
2[B
4O
5(OH)
4]+5H
2O。
Step 3: to discharging through taking off the flue gas that boron handles: the demister 17 at the top through taking off the flue gas self-absorption reaction tower 7 that boron handles is expelled to electric heater 14, and flue gas improves through electric heater 14 temperature after blower fan 15, chimney 16 dischargings.
Be added with oxidant in the sodium hydroxide solution of described absorption reaction tower 7, this oxidant is converted into nitrogen dioxide with part nitric oxide in the flue gas, and this oxidant also can be oxidized to nitrogen with excessive N Hx based component.
SNCR denitrating tower 1 among the present invention is arranged on the tank furnace exit, and flue gas is 850～1100 ℃ with temperature and enters in the SNCR denitrating tower 1.NH3 that reacts in SNCR denitrating tower 1 and the mol ratio of NOx are 1～2, do not need catalyst, have avoided because of boron oxide and half-cooked material dust covering Problem of Failure.Reducing agent is urea or the ammoniacal liquor that contains the NHx base, and the reaction time was greater than 0.5 second.This method nitride treatment effect reaches more than 60%, and behind the oxidant reaction of cooperation rear end, treatment effect reaches more than 80%.
Water cooling tower 4 leading portion flues keep flue-gas temperature more than 500 ℃, and purpose is for preventing sodium salt material dirt and half-cooked material and the boride sticking wall at pipeline, and this method must not heat, and only needs suitably to adjust heat-insulation layer and gets final product.The injection flow rate of water cooling tower 4 control liquid-gas ratio is greater than 5L/Nm3, and the exhanst gas outlet temperature is controlled at 55-70 ℃, and boride is washed in the recirculated water in a large number in this process, soot dust granule thing (half-cooked material) etc. fully brought in first circulatory pool 5 by current.
Flue gas temperature in flue and smoke stack emission process further reduces, and has condensed water to occur.On the one hand, heater was set before chimney, flue-gas temperature suitably can be improved discharging; On the other hand, the demist drainage arrangement is set, pours condensate water into the circulating water pool reuse in flue, chimney bottom; Simultaneously, suitably keep a certain amount of condensate water and in flue, chimney, flow, help to wash the boride crystallization, prevent to stop up.
In the present embodiment the tank furnace smoke processing system is arranged under the tank furnace, down pass and up chimney can carry out heat exchange naturally, have reduced the electrical heating amount of discharging flue gas, the energy-conservation energy.
The above is not the whole or unique embodiment of the present invention, and the conversion of any equivalence that those of ordinary skills take technical solution of the present invention by reading specification of the present invention is claim of the present invention and contains.
Claims (10)
1. tank furnace smoke processing system, it comprises denitrating system, takes off boron system, flue gas emission, it is characterized in that:
Described denitrating system comprises SNCR denitration section (1), the urea liquid storage tank (2) that is connected with SNCR denitration section (1) and measuring pump (3), and wherein SNCR denitration section (1) is arranged on the tank furnace exhanst gas outlet pipeline;
The described boron system of taking off comprises water cooling tower (4), first circulatory pool (5), first circulating pump (6), absorption reaction tower (7), second circulatory pool (8), second circulating pump (9), alkali lye preparing tank (10), alkali lye supply pump (11), efflux pump (12) and centrifuge (13), wherein
Water cooling tower (4) is connected with SNCR denitration section (1) by flue, first circulatory pool (5) is connected by the bottom of fluid pipeline with water cooling tower (4), first circulating pump (6) is connected with first circulatory pool (5) by fluid pipeline, and this first circulating pump (6) is connected to the top of water cooling tower (4) by fluid pipeline;
The bottom of absorption reaction tower (7) is connected with water cooling tower (4) top by flue, second circulatory pool (8) is connected by the bottom of fluid pipeline with absorption reaction tower (7), second circulating pump (9) is connected with second circulatory pool (8) by fluid pipeline, and this second circulating pump (9) is connected to the top of absorption reaction tower (7) by fluid pipeline, alkali lye preparing tank (10) is connected with alkali lye supply pump (11) by fluid pipeline, and alkali lye supply pump (11) is connected with second circulatory pool (8) by fluid pipeline;
Efflux pump (12) is connected with second circulatory pool (8) by fluid pipeline, and this efflux pump (12) is connected with centrifuge (13) by fluid pipeline;
Described flue gas emission comprises electric heater (14), blower fan (15) and chimney (16), wherein electric heater (14) is connected by the top of flue with absorption reaction tower (7), blower fan (15) is connected with electric heater (14) by flue, and chimney (16) is connected with the blowing mouth of blower fan (15).
2. tank furnace smoke processing system as claimed in claim 1 is characterized in that: described second circulatory pool (8) is connected with first circulating pump (6) by fluid pipeline, and wherein fluid pipeline is provided with by-pass valve control.
3. tank furnace smoke processing system as claimed in claim 1, it is characterized in that: this tank furnace smoke processing system also comprises by-pass flue (18), one end of this by-pass flue (18) is connected the outlet of SNCR denitration section (1), and the other end of this by-pass flue (18) is connected the outlet of electric heater (14).
4. tank furnace smoke processing system as claimed in claim 1 is characterized in that: the top exit of described absorption reaction tower (7) is provided with demister (17).
5. tank furnace smoke processing system as claimed in claim 1 is characterized in that: described SNCR denitration section (1) flue before is provided with heat-insulation layer; Flue between described SNCR denitration section (1) and the water cooling tower (4) is provided with heat-insulation layer equally.
6. the flue gas processing method of a tank furnace smoke processing system as claimed in claim 1, it is characterized in that: described method is carried out according to following steps:
Step 1: remove the NO gas in the flue gas: 850 ℃-1100 ℃ tank furnace flue gas enters SNCR denitration section, and measuring pump sprays into SNCR denitration section with the urea liquid of urea liquid storage tank, and the NO gas in urea and the flue gas reacts, and generates the nitrogen G﹠W;
Step 2: to removing NO
xFlue gas takes off boron to be handled:
At first, flue gas enters water cooling tower, spray cooling solution in first circulatory pool is delivered to water cooling tower top by first circulating pump, flue gas is carried out damping cooling and the most of washing of boron compound is entered in the spray solution by the spray cooling solution, be disposed in first circulatory pool, the spray cooling solution is constantly circulation between first circulatory pool and water cooling tower again; Wherein flue gas enters the water cooling tower inlet temperature more than 500 ℃, and flue gas is discharged the water cooling tower outlet temperature at 55-70 ℃, and the control liquid-gas ratio is 5-10L/Nm3; The spray cooling solution is constantly circulation between first circulatory pool and water cooling tower, waits to spray when institute's boron-containing compound reaches finite concentration in the cooling solution entering in second circulatory pool by first circulating pump;
Subsequently, flue gas is discharged again from the top that sprays cooling tower, and the bottom of self-absorption reaction tower enters the absorption reaction tower, sodium hydroxide solution in the alkali lye preparing tank is delivered in second circulatory pool by the alkali lye supply pump, be delivered to the top of absorption reaction tower again by second circulating pump, contact with flue gas adverse current at the absorption reaction tower, sodium hydroxide solution with flow back in second circulatory pool after flue gas contacts, the pH value of control sodium hydroxide solution is 8＜pH＜9, making the product in second circulatory pool is borax, when the borax soln in second circulatory pool reaches finite concentration, drain into centrifuge by efflux pump and carry out centrifugally, isolate the solid borax, liquid is back to second circulatory pool;
Step 3: to discharging through taking off the flue gas that boron handles: the demister at the top through taking off the flue gas self-absorption reaction tower that boron handles is expelled to electric heater, and flue gas improves through the electric heater temperature after blower fan, smoke stack emission.
7. flue gas processing method as claimed in claim 6 is characterized in that: the chemical equation of the chemical reaction that takes place in second circulatory pool in the described step 2 is:
4H
3BO
3+2NaOH＝Na
2[B
4O
5(OH)
4]+5H
2O。
8. flue gas processing method as claimed in claim 6 is characterized in that: be added with oxidant in the sodium hydroxide solution of described absorption reaction tower, this oxidant is converted into nitrogen dioxide with part nitric oxide in the flue gas.
9. flue gas processing method as claimed in claim 6 is characterized in that: the injection flow rate control liquid-gas ratio of described water cooling tower is 5-10L/Nm
3, the exhanst gas outlet temperature is controlled at 55-70 ℃.
10. flue gas processing method as claimed in claim 6, it is characterized in that: described flue gas enters the surface temperature of water cooling tower (4) flue before more than 500 ℃, described flue gas enters the surface temperature of the flue before the SNCR denitration section more than 800 ℃, and described flue gas is 8-11m/s entering SNCR denitration section to the flow velocity in the flue that enters water cooling tower (4).
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| CN103212283A (en) * | 2013-05-07 | 2013-07-24 | 苏圣科技（无锡）有限公司 | Glass tank flue gas treatment system |
| CN104105673A (en) * | 2012-03-05 | 2014-10-15 | 日本电气硝子株式会社 | Discharge gas treatment method and discharge gas treatment device |
| CN104634126A (en) * | 2015-02-28 | 2015-05-20 | 洛阳理工学院 | Treatment apparatus and method of high-boron high-fluoride flue gas for glass melting furnaces |
| CN105003912A (en) * | 2015-07-24 | 2015-10-28 | 湖南高华环保股份有限公司 | Low-NOx combustion method and low-NOx combustion system |
| CN108786408A (en) * | 2018-08-17 | 2018-11-13 | 深圳市凯盛科技工程有限公司 | Thin float glass substrate production line denitrating flue gas boron removal dust removal integrated plant |
| CN110296613A (en) * | 2019-07-26 | 2019-10-01 | 启明星宇节能科技股份有限公司 | A kind of aluminium stone kiln low nitrogen burning equipment and its operation method |
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| CN104105673A (en) * | 2012-03-05 | 2014-10-15 | 日本电气硝子株式会社 | Discharge gas treatment method and discharge gas treatment device |
| CN104105673B (en) * | 2012-03-05 | 2016-05-18 | 日本电气硝子株式会社 | Waste gas processing method and emission-control equipment |
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| CN103212283B (en) * | 2013-05-07 | 2015-07-22 | 苏圣科技（无锡）有限公司 | Glass tank flue gas treatment system |
| CN104634126A (en) * | 2015-02-28 | 2015-05-20 | 洛阳理工学院 | Treatment apparatus and method of high-boron high-fluoride flue gas for glass melting furnaces |
| CN105003912A (en) * | 2015-07-24 | 2015-10-28 | 湖南高华环保股份有限公司 | Low-NOx combustion method and low-NOx combustion system |
| CN105003912B (en) * | 2015-07-24 | 2017-10-27 | 湖南高华环保股份有限公司 | Low nox combustion method and low nox combustion system |
| CN108786408A (en) * | 2018-08-17 | 2018-11-13 | 深圳市凯盛科技工程有限公司 | Thin float glass substrate production line denitrating flue gas boron removal dust removal integrated plant |
| CN110296613A (en) * | 2019-07-26 | 2019-10-01 | 启明星宇节能科技股份有限公司 | A kind of aluminium stone kiln low nitrogen burning equipment and its operation method |
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Effective date of registration: 20160308 Address after: 712021 Rainbow Road, Shaanxi, Xianyang, No. 1 Patentee after: IRICO Group Corp. Address before: 712021 Rainbow Road, Shaanxi, Xianyang, No. 1 Patentee before: Shaanxi Caihong Electronic Glass Co., Ltd. |