CN103432877B - The method of hypergravity complexing ferrous flue-gas wet dust removal desulfurization denitration demercuration dearsenification integration - Google Patents

The method of hypergravity complexing ferrous flue-gas wet dust removal desulfurization denitration demercuration dearsenification integration Download PDF

Info

Publication number
CN103432877B
CN103432877B CN201310403655.9A CN201310403655A CN103432877B CN 103432877 B CN103432877 B CN 103432877B CN 201310403655 A CN201310403655 A CN 201310403655A CN 103432877 B CN103432877 B CN 103432877B
Authority
CN
China
Prior art keywords
denitration
hypergravity machine
dust
sulfide
removal
Prior art date
Application number
CN201310403655.9A
Other languages
Chinese (zh)
Other versions
CN103432877A (en
Inventor
余国贤
黄泽朔
潘威
李海峰
路平
吴宏观
隋志军
万昆
Original Assignee
武汉国力通能源环保有限公司
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by 武汉国力通能源环保有限公司 filed Critical 武汉国力通能源环保有限公司
Priority to CN201310403655.9A priority Critical patent/CN103432877B/en
Publication of CN103432877A publication Critical patent/CN103432877A/en
Application granted granted Critical
Publication of CN103432877B publication Critical patent/CN103432877B/en

Links

Abstract

The invention discloses the method for a kind of hypergravity complexing ferrous flue-gas wet dust removal desulfurization denitration demercuration dearsenification integration.The present invention first utilizes inorganic sulphide to absorb SOx,, trapped by the grit in flue gas, inorganic sulphide is with raw insoluble one-tenth sulphurizing salts of toxic heavy metal reaction such as the mercury in flue gas, arsenic meanwhile, then utilize complexing ferrous absorption NOx, inorganic sulphide is as reducing agent absorbent regeneration.The present invention adopts hypergravity machine as gas-liquid mass transfer strengthening device, is conducive to removing of the Toxics such as dust, SOx, NOx, mercury, arsenic.Present invention process is simple, and absorption efficiency is high, and dedusting is thorough, and desulfurization degree is more than 99%, and denitration rate, more than 96%, can remove dust, mercury and the arsenic in flue gas substantially completely.

Description

The method of hypergravity complexing ferrous flue-gas wet dust removal desulfurization denitration demercuration dearsenification integration

Technical field

The present invention relates to industrial flue gas cleaning, refer to the method for a kind of hypergravity complexing ferrous flue-gas wet dust removal desulfurization denitration demercuration dearsenification integration particularly.

Background technology

The pollution of acid rain and the harm caused thereof have become one of important environmental problem paid close attention to whole world various countries.China take coal as the country of main energy sources, adds up according to investigations, the SO of China more than 90% 2, more than 67% NO x, more than 70% the discharge capacity of flue dust all come from burning of coal.And the SO that coal combustion produces 2and NO xit is the main source that industrial waste gas pollutes (acid rain harm).Nitrogen oxide also can form photochemical pollution, produces greenhouse effects, damages the ozone layer, have the harm such as toxic action processed to human body.Nitrogen oxide and oxysulfide also can be converted into PM2.5 and cause haze weather.

The whole world mercury total amount be discharged into every year in air has more than 5000 ton, and wherein about 4000 tons is artificial result, and the mercury emission of coal-fired process accounts for more than 30%.In China's raw coal, mercury content excursion is at 0.1 ~ 5.5mg/Kg, average mercury content 0.22mg/Kg.Because the yearly consumption of China's fire coal is huge, the amount of annual coal fire discharged mercury and pollutant thereof is all very surprising, the current mercury emission of China exceedes the U.S., and growth rate is very fast, constitute grave danger to human health and ecological environment, the discharge capacity therefore controlling Mercury In Coal Combustion Flue Gas is significant.During coal combustion, mercury major part enters air with flue gas, and what enter lime-ash only accounts for fraction, wherein accounts for 23.1% ~ 26.9% in flying dust, accounts for 56.3% ~ 69.7% in flue gas, and the mercury entering lime-ash only accounts for about 2%.Therefore controlling coal-fired mercury pollution key is that the mercury controlled in flue gas discharges in air.Oxidant SO stronger in flue gas 2, NO 2, Cl 2etc. simple substance and the oxide existence form that obviously can affect mercury metal.Along with the increase of oxidant, too increase the oxide components of mercury, as HgCl 2, HgSO 4deng.

Mercury In Coal Combustion Flue Gas belongs to trace level pollutant, wherein mainly contains three kinds of forms: gaseous elemental mercury, gaseous oxidation mercury, solid granulates mercury.Wherein gaseous elemental mercury is the main existence form of mercury in flue gas.The existing forms of mercury in flue gas has removed material impact to mercury.The principal element affecting mercury in flue gas existing forms has coal-fired kind, ignition temperature, smoke components etc.Physics, the chemical property of mercury species differ greatly.As soluble in water in gaseous oxidation mercury, and easily adsorbed by the particle in flue gas, therefore easily removed by wet desulphurization equipment or cleaner, particle mercury is also easily removed by deduster, contrary atomic state mercury volatility is high, water-soluble low, is difficult to be desulfurized or cleaner is caught, and almost all discharges into the atmosphere, and mean residence time reached half a year by 2 years in an atmosphere, the conveying of logical long-distance forms mercury pollution widely very easily in an atmosphere.Atomic state mercury is form the most rambunctious, is also the difficult point of coal-fired flue gas mercury removal.

Dedusting refers to the separation operation process the multiphase mixture of gas and dust particle.As the grit diameter of object of dust removal, generally at the grit of 0.01 ~ 100 μm.The grit of more than 100 μm falls sedimentation very soon due to Action of Gravity Field; And more than 10 μm grits are easy to be separated, problem is little; The grit of 0.1 ~ 10 μm, particularly the grit of less than 1 μm is separated comparatively difficulty, and being also harmful to human body, is current main research range.From the angle of environmental protection, dust is the formidable enemy of health.Especially the floating dust of particle diameter between 0.5 ~ 5 μm (i.e. the long-term dust even floated in an atmosphere for several years), maximum to the harm of people.Be greater than the grit of 5 μm, due to effect of inertia, can be got rid of by vibrissa and respiratory mucus, be less than the floating dust of 0.5 μm, also can discharge with phlegm because gas diffusion is adhered to upper respiratory tract surface.The floating dust of 0.5 ~ 5 μm directly arrives lung by respiratory tract and deposits only, harmful to human.

At present, what industrial employing was more is selective catalytic reduction, namely adopts ammonia or urea to make reducing agent and NO is reduced to nitrogen, as patent USPatent4,221,768, SwedishPatent8404840-4, USPatent4,101,238, USPatent4,048, the method disclosed in 112.But said method needs (about 350 DEG C) at relatively high temperatures just can carry out, and catalyst price is higher, easy poisoning and deactivation, can not realize desulphurization denitration simultaneously.Japan Patent P1659565j (1976), P181759c (1976), P63100918, A2 (1988) remove NO while proposing xand SO 2method adopt oxidant NO is oxidized to NO soluble in water 2, as chloric acid, potassium permanganate, hydrogen peroxide, ozone etc., but liquid phase oxidation is failed popularization and is come due to high in cost of production reason.The yellow phosphorus method (see document Nature, 1990,343 (11): 151-153) that California, USA university Berkeley laboratory proposes, can remove the NO in flue gas simultaneously xand SO 2, but belong to and entirely abandon method.This method will consume a large amount of phosphor resources, and its toxicity is large, and operation requirements is higher.

Fe (II)-EDTA (EDTA represents disodium ethylene diamine tetraacetate) is adopted to remove NO in waste gas.The reaction equation of Fe (II) EDTA and NO is as follows:

Fe(II)EDTA+NO→Fe(II)EDTA(NO)(1)

In nearly three ten years afterwards, many scholars have carried out comparatively systematic research to this reaction, but have not yet to see industrialization report, and the greatest problem affecting wet process complex denitration application is the cycle applications of absorbing liquid.

The circulation regeneration method of absorbing liquid mainly contains bioanalysis, improves the three major types such as absorbent absorbability and electrolysis, wherein applies the most extensive to improve absorbent absorbability.Fe (II) EDTA is easily oxidized to Fe (III) EDTA, and Fe (III) EDTA can not complexing NO, and absorption efficiency is declined rapidly.Regenerate Fe (II) by biocatalytic reduction method, but this method is just in the exploratory stage at present, large-scale application will be obtained also have many problems to need to solve in waste gas pollution control and treatment process.In the application of reducing agent, hydrazine and H 2s reduces Fe (III) EDTA, strengthens the assimilation effect of EDTA Fe, but due to H 2s and hydrazine are all poisonous, are difficult to industrially apply.Someone adopts tannic acid, pyrogaelol and gallic acid to do the second additive to strengthen the absorptive capacity of Fe (II) EDTA, NO in two hours xremoval efficiency remain on 60 ~ 65% always, effectively improve the reduction effect of poly-phenol mixture.Also someone reports dithionic acid sodium reduction Fe (III) EDTA, and reduction effect is better.Domestic scholars reports reducing/regenerating Fe (III) EDTA such as iron filings, malic acid, vitamin C, but the key issue of this technology to be operating cost high, process route is complicated, also needs further research.

Summary of the invention

Object of the present invention is exactly to overcome the deficiency existing for prior art, provides the method for a kind of hypergravity complexing ferrous flue-gas wet dust removal desulfurization denitration demercuration dearsenification integration.

The method of hypergravity complexing of the present invention ferrous flue-gas wet dust removal desulfurization denitration demercuration dearsenification integration, comprises the following steps:

1) by temperature be 40 DEG C ~ 120 DEG C and send into dust-removal and desulfurizing hypergravity machine containing SOx, NOx, mercury, arsenic flue gas, the concentration being 0 DEG C ~ 40 DEG C with the temperature entering dust-removal and desulfurizing hypergravity machine is sulfide solution counter current contacting in dust-removal and desulfurizing hypergravity machine rotor packing layer of 0.01 ~ 4.0mol/L, dedusting, desulfurization, demercuration, dearsenification; Described sulfide is selected from vulcanized sodium, NaHS, ammonium sulfide, ammonium hydro sulfide, potassium sulfide or potassium bisulfide;

2) denitration hypergravity machine is entered with the reacted flue gas of sulfide solution from dust-removal and desulfurizing hypergravity machine gaseous phase outlet, be absorbent counter current contacting in denitration hypergravity machine rotor packing layer of 0 DEG C ~ 55 DEG C again with the temperature entering denitration hypergravity machine, reaction denitration; Wherein, described absorbent contains complexing ferrous iron and sulfide reducing agent, the complexing agent of described complexing ferrous iron is selected from ethylenediamine tetra-acetic acid (EDTA), N-(2-ethoxy) ethylenediamine-N, N', one or both mixture in N'-triacetic acid (HEDTA), nitrilotriacetic acid (NTA), diethylene triamine pentacetic acid (DTPA) (DTPA), citric acid, described sulfide reducing agent is selected from vulcanized sodium, NaHS, ammonium sulfide, ammonium hydro sulfide, potassium sulfide or potassium bisulfide; Reacted purified gas enters demister from denitration hypergravity machine gaseous phase outlet, enters exhaust system subsequently;

3) after compensator, enter desulfurization subsider from dust-removal and desulfurizing hypergravity machine liquid out, by sulphur wherein, insoluble sulphurizing salt, ash fall to bottom, after filter filters, reclaim solid, filtrate returns desulfurization subsider;

4) clear liquid on desulfurization subsider top is extracted out and is sent to dust-removal and desulfurizing hypergravity machine, flows to dust-removal and desulfurizing hypergravity machine together, carry out cyclic absorption desulfurization with after the sulfide on-line mixing of supplementing;

5) after compensator, enter denitration subsider from denitration hypergravity machine liquid out, by sulphur wherein, insoluble sulfuration salt settling to bottom, after filter filters, reclaim solid, filtrate returns denitration subsider;

(6) clear liquid on denitration subsider top is extracted out and is sent to denitration hypergravity machine, flows to denitration hypergravity machine together, carry out cyclic absorption denitration with after the sulfide reducing agent on-line mixing of supplementing.

In the present invention, in described absorbent, total Fe concentration is 0.01mol/L ~ 0.5mol/L, and the mol ratio of sulfide and total Fe is 3:1 ~ 5:1, and the mol ratio of described complexing agent and total Fe is 1.02:1 ~ 2:1, and described total Fe refers to Fe 2+and Fe 3+sum.Described sulfide is preferably ammonium sulfide or ammonium hydro sulfide.

In the present invention, the complexing agent of described complexing ferrous iron is preferably the mixture of EDTA and citric acid, the mixture of HEDTA and citric acid, the mixture of EDTA and HEDTA or the mixture of NTA and DTPA.It is that to mix optimum weight ratio be 1:1 ~ 1:3 for 1:1 ~ 1:3, NTA and DTPA that EDTA and citric acid mixing optimum weight ratio to be 1:2 ~ 1:4, HEDTA with citric acid mixing optimum weight ratio be 1:3 ~ 1:6, EDTA and HEDTA mixes optimum weight ratio.

Beneficial effect of the present invention is: first utilize inorganic sulphide to absorb SOx, simultaneously, by in flue gas more than 99% grit trap, inorganic sulphide is with raw insoluble one-tenth sulphurizing salts of toxic heavy metal reaction such as the mercury in flue gas, arsenic, then utilize complexing ferrous absorption NOx, inorganic sulphide is as reducing agent absorbent regeneration.The present invention adopts hypergravity machine as gas-liquid mass transfer strengthening device, is conducive to removing of the Toxics such as dust, SOx, NOx, mercury, arsenic.

The present invention is in desulfurization, inorganic sulphide is adopted to absorb SOx, not only can obtain sulphur, the heavy metals such as mercury, arsenic and lead are converted into insoluble sulfide precipitation simultaneously and trap from flue gas, the sulphite produced in desulfurization and thiosulfate may be used for producing the sulfide as reducing agent.

The present invention is in denitration, and adopt cheap inorganic sulphide, Complexing Iron can not only be reduced to complexing ferrous iron, and the NO of complexed absorption can be reduced to nitrogen, the regeneration efficiency of absorbent is high, absorbing liquid application capable of circulation.The product sulphur of the oxidized generation of reducing agent inorganic sulphide, can reclaim, and is processed as high-quality sulfur product, can not produce secondary pollution.Reducing agent is cheap and easy to get, and the sulphite high temperature reduction produced in desulfurization can be utilized to be sulphurizing salt.

Can by under the dust arrestment of the overwhelming majority in sweetening process, after hypergravity denitration, the pollutant in flue gas substantially all removes, and the degree of purification of flue gas is high.Sulfureous in flue gas oxygenate conversion is sulphite and thiosulfate, can also produce thiosulfate further, sells as accessory substance.

Present invention process is simple, and absorption efficiency is high, and dedusting is thorough, and desulfurization degree is more than 99%, and denitration rate, more than 96%, can remove dust, mercury and the arsenic in flue gas substantially completely.

Accompanying drawing explanation

Fig. 1 is the process chart of hypergravity complexing of the present invention ferrous flue-gas wet dust removal desulfurization denitration demercuration dearsenification integration.

Detailed description of the invention

In order to explain the present invention better, below in conjunction with the drawings and specific embodiments, the present invention is described in further detail, but they do not form restriction to the present invention.

The size of two hypergravity machines of the present invention's test: rotor interior diameter 250mm, rotor outside diameter 600mm, rotor height 100mm.

Embodiment 1

The method of hypergravity complexing ferrous flue-gas wet dust removal desulfurization denitration demercuration dearsenification integration, as shown in Figure 1, comprises the following steps:

1) be that the flue gas of 120 DEG C is with 400Nm by dedusting temperature 3the flow velocity of/h sends into dust-removal and desulfurizing hypergravity machine, SO in flue gas 2concentration is 600 ~ 1000ppmv, NO concentration is 500 ~ 800ppmv, dust content 700 ~ 1100mg/Nm 3, arsenic content 6 ~ 20 μ g/Nm 3, mercury content 9 ~ 17 μ g/Nm 3, oxygen concentration 2%v, flue gas with squeeze into through pump sodium sulfide solution counter current contacting in hypergravity machine rotor packing layer that temperature in dust-removal and desulfurizing hypergravity is 20 DEG C by storage tank, dedusting, desulfurization, demercuration, dearsenification, flue gas and sodium sulfide solution volume ratio are 50:1, and the concentration of sodium sulfide solution is 0.01mol/L;

2) enter denitration hypergravity machine with the reacted flue gas of sodium sulfide solution from dust-removal and desulfurizing hypergravity machine gaseous phase outlet, then be absorbent counter current contacting in denitration hypergravity machine rotor packing layer of 20 DEG C with the temperature entering denitration hypergravity machine, reaction denitration; Wherein, absorbent consists of vulcanized sodium, HEDTA complexing is ferrous, and total Fe concentration is the mol ratio 1.02:1 of 0.01mol/L, HEDTA and total Fe, and the mol ratio of vulcanized sodium and total iron is 5:1, and the volume ratio of flue gas and absorbent is 100:1; Reacted purified gas enters demister from denitration hypergravity machine gaseous phase outlet, enters exhaust system subsequently; Purified gas adopts infrared spectrometer to detect, SO in purified gas 2concentration is 5ppmv, NO concentration is 7ppmv, dust content <1mg/Nm 3, adopt atomic absorption spectrography (AAS) to detect heavy metal, can't detect arsenic, mercury;

3) after compensator, enter desulfurization subsider from dust-removal and desulfurizing hypergravity machine liquid out, by sulphur wherein, insoluble sulphurizing salt, ash fall to bottom, after filter filters, reclaim solid, filtrate returns desulfurization subsider;

4) clear liquid on desulfurization subsider top is extracted out and is sent to dust-removal and desulfurizing hypergravity machine, flows to dust-removal and desulfurizing hypergravity machine together, carry out cyclic absorption desulfurization with after the sulfide on-line mixing of supplementing;

5) after compensator, enter denitration subsider from denitration hypergravity machine liquid out, by sulphur wherein, insoluble sulfuration salt settling to bottom, after filter filters, reclaim solid, filtrate returns denitration subsider;

(6) clear liquid on denitration subsider top is extracted out and is sent to denitration hypergravity machine, flows to denitration hypergravity machine together, carry out cyclic absorption denitration with after the sulfide reducing agent on-line mixing of supplementing.

Embodiment 2

The method of hypergravity complexing ferrous flue-gas wet dust removal desulfurization denitration demercuration dearsenification integration, as shown in Figure 1, comprises the following steps:

1) be that 40 DEG C of flue gases are with 400Nm by temperature 3the flow velocity of/h sends into dust-removal and desulfurizing hypergravity machine, SO in flue gas 2concentration is 1400 ~ 2000ppmv, NO concentration is 500 ~ 800ppmv, dust content 700 ~ 1100mg/Nm 3, arsenic content 6 ~ 20 μ g/Nm 3, mercury content 9 ~ 17 μ g/Nm 3, oxygen concentration 3%v, flue gas with squeeze into through pump NaHS aqueous solution counter current contacting in hypergravity machine rotor packing layer that temperature in dust-removal and desulfurizing hypergravity is 0 DEG C by storage tank, dedusting, desulfurization, demercuration, dearsenification, the volume ratio of flue gas and the NaHS aqueous solution is 700:1, and the concentration of the NaHS aqueous solution is 1.0mol/L;

2) flue gas and after NaHS reactant aqueous solution enters denitration hypergravity machine from dust-removal and desulfurizing hypergravity machine gaseous phase outlet, then is absorbent counter current contacting in denitration hypergravity machine rotor packing layer of 0 DEG C with the temperature entering denitration hypergravity machine, reaction denitration; Wherein, absorbent consists of NaHS, EDTA complexing is ferrous, and total Fe concentration is the mol ratio 1.5:1 of 0.5mol/L, EDTA and total Fe, and the mol ratio of NaHS and total iron is 4:1, and the volume ratio of flue gas and absorbent is 500:1; Reacted purified gas enters demister from denitration hypergravity machine gaseous phase outlet, enters exhaust system subsequently; Purified gas adopts infrared spectrometer to detect, SO in purified gas 2concentration is 10ppmv, NO concentration is 17ppmv, dust content <1mg/Nm 3, adopt atomic absorption spectrography (AAS) to detect heavy metal, can't detect arsenic, mercury;

3) after compensator, enter desulfurization subsider from dust-removal and desulfurizing hypergravity machine liquid out, by sulphur wherein, insoluble sulphurizing salt, ash fall to bottom, after filter filters, reclaim solid, filtrate returns desulfurization subsider;

4) clear liquid on desulfurization subsider top is extracted out and is sent to dust-removal and desulfurizing hypergravity machine, flows to dust-removal and desulfurizing hypergravity machine together, carry out cyclic absorption desulfurization with after the sulfide on-line mixing of supplementing;

5) after compensator, enter denitration subsider from denitration hypergravity machine liquid out, by sulphur wherein, insoluble sulfuration salt settling to bottom, after filter filters, reclaim solid, filtrate returns denitration subsider;

(6) clear liquid on denitration subsider top is extracted out and is sent to denitration hypergravity machine, flows to denitration hypergravity machine together, carry out cyclic absorption denitration with after the sulfide reducing agent on-line mixing of supplementing.

Embodiment 3

The method of hypergravity complexing ferrous flue-gas wet dust removal desulfurization denitration demercuration dearsenification integration, as shown in Figure 1, comprises the following steps:

1) be that 80 DEG C of flue gases are with 400Nm by temperature 3the flow velocity of/h sends into dust-removal and desulfurizing hypergravity machine, SO in flue gas 2concentration is 1600 ~ 2400ppmv, NO concentration is 500 ~ 800ppmv, dust content 700 ~ 1100mg/Nm 3, arsenic content 6 ~ 20 μ g/Nm 3, mercury content 9 ~ 17 μ g/Nm 3, oxygen concentration 5%v, flue gas with squeeze into through pump ammonium sulfide solution counter current contacting in hypergravity machine rotor packing layer that temperature in dust-removal and desulfurizing hypergravity is 35 DEG C by storage tank, dedusting, desulfurization, demercuration, dearsenification, the volume ratio of flue gas and ammonium sulfide solution is 800:1, and the concentration of ammonium sulfide solution is 2.0mol/L;

2) enter denitration hypergravity machine with the reacted flue gas of ammonium sulfide solution from dust-removal and desulfurizing hypergravity machine gaseous phase outlet, then be absorbent counter current contacting in denitration hypergravity machine rotor packing layer of 55 DEG C with the temperature entering denitration hypergravity machine, reaction denitration; Wherein, absorbent consists of ammonium sulfide, NTA complexing is ferrous, and total Fe concentration is the mol ratio 2:1 of 0.3mol/L, NTA and total Fe, and the mol ratio of ammonium sulfide and total iron is 3:1, and the volume ratio of flue gas and absorbent is 1000:1; Reacted purified gas enters demister from denitration hypergravity machine gaseous phase outlet, enters exhaust system subsequently; Purified gas adopts infrared spectrometer to detect, SO in purified gas 2concentration is 12ppmv, NO concentration is 15ppmv, dust content <1mg/Nm 3, adopt atomic absorption spectrography (AAS) to detect heavy metal, can't detect arsenic, mercury;

3) after compensator, enter desulfurization subsider from dust-removal and desulfurizing hypergravity machine liquid out, by sulphur wherein, insoluble sulphurizing salt, ash fall to bottom, after filter filters, reclaim solid, filtrate returns desulfurization subsider;

4) clear liquid on desulfurization subsider top is extracted out and is sent to dust-removal and desulfurizing hypergravity machine, flows to dust-removal and desulfurizing hypergravity machine together, carry out cyclic absorption desulfurization with after the sulfide on-line mixing of supplementing;

5) after compensator, enter denitration subsider from denitration hypergravity machine liquid out, by sulphur wherein, insoluble sulfuration salt settling to bottom, after filter filters, reclaim solid, filtrate returns denitration subsider;

(6) clear liquid on denitration subsider top is extracted out and is sent to denitration hypergravity machine, flows to denitration hypergravity machine together, carry out cyclic absorption denitration with after the sulfide reducing agent on-line mixing of supplementing.

Embodiment 4

The method of hypergravity complexing ferrous flue-gas wet dust removal desulfurization denitration demercuration dearsenification integration, as shown in Figure 1, comprises the following steps:

1) be that 60 DEG C of flue gases are with 400Nm by the temperature after dedusting 3the flow velocity of/h sends into dust-removal and desulfurizing hypergravity machine, SO in flue gas 2concentration is 600 ~ 1000ppmv, NO concentration is 800 ~ 1200ppmv, dust content 700 ~ 1100mg/Nm 3, arsenic content 6 ~ 20 μ g/Nm 3, mercury content 9 ~ 17 μ g/Nm 3, oxygen concentration 6%v, flue gas with squeeze into through pump ammonium hydro sulfide aqueous solution counter current contacting in hypergravity machine rotor packing layer that temperature in desulfurization hypergravity is 40 DEG C by storage tank, dedusting, desulfurization, demercuration, dearsenification, the volume ratio of flue gas and the ammonium hydro sulfide aqueous solution is 800:1, and the concentration of the ammonium hydro sulfide aqueous solution is 3.0mol/L;

2) flue gas and after ammonium hydro sulfide reactant aqueous solution enters denitration hypergravity machine from dust-removal and desulfurizing hypergravity machine gaseous phase outlet, then is absorbent counter current contacting in denitration hypergravity machine rotor packing layer of 45 DEG C with the temperature entering denitration hypergravity machine, reaction denitration; Wherein, absorbent consists of ammonium hydro sulfide, DTPA complexing is ferrous, and total Fe concentration is the mol ratio 1.2:1 of 0.3mol/L, DTPA and total Fe, and the mol ratio of ammonium hydro sulfide and total iron is 3:1, and the volume ratio of flue gas and absorbent is 800:1; Reacted purified gas enters demister from denitration hypergravity machine gaseous phase outlet, enters exhaust system subsequently; Purified gas adopts infrared spectrometer to detect, SO in purified gas 2concentration is 5ppmv, NO concentration is 20ppmv, dust content <1mg/Nm 3, adopt atomic absorption spectrography (AAS) to detect heavy metal, can't detect arsenic, mercury;

3) after compensator, enter desulfurization subsider from dust-removal and desulfurizing hypergravity machine liquid out, by sulphur wherein, insoluble sulphurizing salt, ash fall to bottom, after filter filters, reclaim solid, filtrate returns desulfurization subsider;

4) clear liquid on desulfurization subsider top is extracted out and is sent to dust-removal and desulfurizing hypergravity machine, flows to dust-removal and desulfurizing hypergravity machine together, carry out cyclic absorption desulfurization with after the sulfide on-line mixing of supplementing;

5) after compensator, enter denitration subsider from denitration hypergravity machine liquid out, by sulphur wherein, insoluble sulfuration salt settling to bottom, after filter filters, reclaim solid, filtrate returns denitration subsider;

(6) clear liquid on denitration subsider top is extracted out and is sent to denitration hypergravity machine, flows to denitration hypergravity machine together, carry out cyclic absorption denitration with after the sulfide reducing agent on-line mixing of supplementing.

Embodiment 5

The method of hypergravity complexing ferrous flue-gas wet dust removal desulfurization denitration demercuration dearsenification integration, as shown in Figure 1, comprises the following steps:

1) be that 75 DEG C of flue gases are with 400Nm by the temperature after dedusting 3the flow velocity of/h sends into dust-removal and desulfurizing hypergravity machine, SO in flue gas 2concentration is 2300 ~ 3100ppmv, NO concentration is 800 ~ 1200ppmv, dust content 700 ~ 1100mg/Nm 3, arsenic content 6 ~ 20 μ g/Nm 3, mercury content 9 ~ 17 μ g/Nm 3, oxygen concentration 6%v, flue gas with squeeze into through pump potassium sulfide aqueous solution counter current contacting in hypergravity machine rotor packing layer that temperature in desulfurization hypergravity is 30 DEG C by storage tank, dedusting, desulfurization, demercuration, dearsenification, the volume ratio of flue gas and potassium sulfide aqueous solution is 800:1, and the concentration of potassium sulfide aqueous solution is 3.0mol/L;

2) enter denitration hypergravity machine with the reacted flue gas of potassium sulfide aqueous solution from dust-removal and desulfurizing hypergravity machine gaseous phase outlet, then be absorbent counter current contacting in denitration hypergravity machine rotor packing layer of 50 DEG C with the temperature entering denitration hypergravity machine, reaction denitration; Wherein, absorbent consists of potassium sulfide, EDTA+ citric acid complex is ferrous, total Fe concentration is 0.2mol/L, the mol ratio 1.3:1 of EDTA+ citric acid and total Fe, EDTA is 1:3 with citric acid mixing optimum weight ratio, the mol ratio of potassium sulfide and total iron is 3:1, and the volume ratio of flue gas and absorbent is 800:1; Reacted purified gas enters demister from denitration hypergravity machine gaseous phase outlet, enters exhaust system subsequently; Purified gas adopts infrared spectrometer to detect, SO in purified gas 2concentration is 6ppmv, NO concentration is 6ppmv, dust content <1mg/Nm 3, adopt atomic absorption spectrography (AAS) to detect heavy metal, can't detect arsenic, mercury;

3) after compensator, enter desulfurization subsider from dust-removal and desulfurizing hypergravity machine liquid out, by sulphur wherein, insoluble sulphurizing salt, ash fall to bottom, after filter filters, reclaim solid, filtrate returns desulfurization subsider;

4) clear liquid on desulfurization subsider top is extracted out and is sent to dust-removal and desulfurizing hypergravity machine, flows to dust-removal and desulfurizing hypergravity machine together, carry out cyclic absorption desulfurization with after the sulfide on-line mixing of supplementing;

5) after compensator, enter denitration subsider from denitration hypergravity machine liquid out, by sulphur wherein, insoluble sulfuration salt settling to bottom, after filter filters, reclaim solid, filtrate returns denitration subsider;

(6) clear liquid on denitration subsider top is extracted out and is sent to denitration hypergravity machine, flows to denitration hypergravity machine together, carry out cyclic absorption denitration with after the sulfide reducing agent on-line mixing of supplementing.

Embodiment 6

The method of hypergravity complexing ferrous flue-gas wet dust removal desulfurization denitration demercuration dearsenification integration, as shown in Figure 1, comprises the following steps:

1) be that 90 DEG C of flue gases are with 400Nm by the temperature after dedusting 3the flow velocity of/h sends into dust-removal and desulfurizing hypergravity machine, SO in flue gas 2concentration is 2300 ~ 3100ppmv, NO concentration is 800 ~ 1200ppmv, dust content 700 ~ 1100mg/Nm 3, arsenic content 6 ~ 20 μ g/Nm 3, mercury content 9 ~ 17 μ g/Nm 3oxygen concentration 7%v, flue gas with squeeze into through pump potassium bisulfide aqueous solution counter current contacting in hypergravity machine rotor packing layer that temperature in desulfurization hypergravity is 20 DEG C by storage tank, dedusting, desulfurization, demercuration, dearsenification, the volume ratio of flue gas and the potassium bisulfide aqueous solution is 1000:1, and the concentration of the potassium bisulfide aqueous solution is 4.0mol/L;

2) flue gas and after potassium bisulfide reactant aqueous solution enters denitration hypergravity machine from dust-removal and desulfurizing hypergravity machine gaseous phase outlet, then is absorbent counter current contacting in denitration hypergravity machine rotor packing layer of 50 DEG C with the temperature entering denitration hypergravity machine, reaction denitration; Wherein, absorbent consists of potassium bisulfide, HEDTA+ citric acid complex is ferrous, total Fe concentration is 0.4mol/L, the mol ratio 1.2:1 of HEDTA+ citric acid and total Fe, HEDTA is 1:5 with citric acid mixing optimum weight ratio, the mol ratio of potassium bisulfide and total iron is 4:1, and the volume ratio of flue gas and absorbent is 800:1; Reacted purified gas enters demister from denitration hypergravity machine gaseous phase outlet, enters exhaust system subsequently; Purified gas adopts infrared spectrometer to detect, SO in purified gas 2concentration is 5ppmv, NO concentration is 5ppmv, dust content <1mg/Nm 3, adopt atomic absorption spectrography (AAS) to detect heavy metal, can't detect arsenic, mercury;

3) after compensator, enter desulfurization subsider from dust-removal and desulfurizing hypergravity machine liquid out, by sulphur wherein, insoluble sulphurizing salt, ash fall to bottom, after filter filters, reclaim solid, filtrate returns desulfurization subsider;

4) clear liquid on desulfurization subsider top is extracted out and is sent to dust-removal and desulfurizing hypergravity machine, flows to dust-removal and desulfurizing hypergravity machine together, carry out cyclic absorption desulfurization with after the sulfide on-line mixing of supplementing;

5) after compensator, enter denitration subsider from denitration hypergravity machine liquid out, by sulphur wherein, insoluble sulfuration salt settling to bottom, after filter filters, reclaim solid, filtrate returns denitration subsider;

(6) clear liquid on denitration subsider top is extracted out and is sent to denitration hypergravity machine, flows to denitration hypergravity machine together, carry out cyclic absorption denitration with after the sulfide reducing agent on-line mixing of supplementing.

Embodiment 7

The method of hypergravity complexing ferrous flue-gas wet dust removal desulfurization denitration demercuration dearsenification integration, as shown in Figure 1, comprises the following steps:

1) be that 85 DEG C of flue gases are with 400Nm by the temperature after dedusting 3the flow velocity of/h sends into dust-removal and desulfurizing hypergravity machine, SO in flue gas 2concentration is 2300 ~ 3100ppmv, NO concentration is 1000 ~ 1500ppmv, dust content 700 ~ 1100mg/Nm 3, arsenic content 6 ~ 20 μ g/Nm 3, mercury content 9 ~ 17 μ g/Nm 3, oxygen concentration 7%v, flue gas with squeeze into through pump sodium sulfide solution counter current contacting in hypergravity machine rotor packing layer that temperature in desulfurization hypergravity is 25 DEG C by storage tank, dedusting, desulfurization, demercuration, dearsenification, the volume ratio of flue gas and sodium sulfide solution is 1000:1, and the concentration of sodium sulfide solution is 1.0mol/L;

2) enter denitration hypergravity machine with the reacted flue gas of sodium sulfide solution from dust-removal and desulfurizing hypergravity machine gaseous phase outlet, then be absorbent counter current contacting in denitration hypergravity machine rotor packing layer of 40 DEG C with the temperature entering denitration hypergravity machine, reaction denitration; Wherein, absorbent consists of vulcanized sodium, EDTA+HEDTA complexing is ferrous, total Fe concentration is 0.15mol/L, the mol ratio 1.2:1 of EDTA+HEDTA and total Fe, it is 1:2 that EDTA and HEDTA mixes optimum weight ratio, the mol ratio of vulcanized sodium and total iron is 3:1, and the volume ratio of flue gas and absorbent is 800:1; Reacted purified gas enters demister from denitration hypergravity machine gaseous phase outlet, enters exhaust system subsequently; Purified gas adopts infrared spectrometer to detect, SO in purified gas 2concentration is 7ppmv, NO concentration is 9ppmv, dust content <1mg/Nm 3, adopt atomic absorption spectrography (AAS) to detect heavy metal, can't detect arsenic, mercury;

3) after compensator, enter desulfurization subsider from dust-removal and desulfurizing hypergravity machine liquid out, by sulphur wherein, insoluble sulphurizing salt, ash fall to bottom, after filter filters, reclaim solid, filtrate returns desulfurization subsider;

4) clear liquid on desulfurization subsider top is extracted out and is sent to dust-removal and desulfurizing hypergravity machine, flows to dust-removal and desulfurizing hypergravity machine together, carry out cyclic absorption desulfurization with after the sulfide on-line mixing of supplementing;

5) after compensator, enter denitration subsider from denitration hypergravity machine liquid out, by sulphur wherein, insoluble sulfuration salt settling to bottom, after filter filters, reclaim solid, filtrate returns denitration subsider;

(6) clear liquid on denitration subsider top is extracted out and is sent to denitration hypergravity machine, flows to denitration hypergravity machine together, carry out cyclic absorption denitration with after the sulfide reducing agent on-line mixing of supplementing.

Embodiment 8

The method of hypergravity complexing ferrous flue-gas wet dust removal desulfurization denitration demercuration dearsenification integration, as shown in Figure 1, comprises the following steps:

1) be that 50 DEG C of flue gases are with 400Nm by the temperature after dedusting 3the flow velocity of/h sends into dust-removal and desulfurizing hypergravity machine, SO in flue gas 2concentration is 2300 ~ 3100ppmv, NO concentration is 800 ~ 1200ppmv, dust content 700 ~ 1100mg/Nm 3, arsenic content 6 ~ 20 μ g/Nm 3, mercury content 9 ~ 17 μ g/Nm 3, oxygen concentration 8%v, flue gas with squeeze into through pump potassium bisulfide aqueous solution counter current contacting in hypergravity machine rotor packing layer that temperature in desulfurization hypergravity is 35 DEG C by storage tank, dedusting, desulfurization, demercuration, dearsenification, the volume ratio of flue gas and the potassium bisulfide aqueous solution is 1000:1, and the concentration of the potassium bisulfide aqueous solution is 3.5mol/L;

2) enter denitration hypergravity machine with the reacted flue gas of sodium sulfide solution from dust-removal and desulfurizing hypergravity machine gaseous phase outlet, then be absorbent counter current contacting in denitration hypergravity machine rotor packing layer of 40 DEG C with the temperature entering denitration hypergravity machine, reaction denitration; Wherein, absorbent consists of vulcanized sodium, DTPA+NTA complexing is ferrous, and total Fe concentration is 0.25mol/L, the mol ratio 1.3:1 of DTPA+NTA and total Fe, it is 1:1 that NTA and DTPA mixes optimum weight ratio, and the mol ratio of vulcanized sodium and total iron is 3:1, and the volume ratio of flue gas and absorbent is 800:1; Reacted purified gas enters demister from denitration hypergravity machine gaseous phase outlet, enters exhaust system subsequently; Purified gas adopts infrared spectrometer to detect, SO in purified gas 2concentration is 5ppmv, NO concentration is 7ppmv, dust content <1mg/Nm 3, adopt atomic absorption spectrography (AAS) to detect heavy metal, can't detect arsenic, mercury;

3) after compensator, enter desulfurization subsider from dust-removal and desulfurizing hypergravity machine liquid out, by sulphur wherein, insoluble sulphurizing salt, ash fall to bottom, after filter filters, reclaim solid, filtrate returns desulfurization subsider;

4) clear liquid on desulfurization subsider top is extracted out and is sent to dust-removal and desulfurizing hypergravity machine, flows to dust-removal and desulfurizing hypergravity machine together, carry out cyclic absorption desulfurization with after the sulfide on-line mixing of supplementing;

5) after compensator, enter denitration subsider from denitration hypergravity machine liquid out, by sulphur wherein, insoluble sulfuration salt settling to bottom, after filter filters, reclaim solid, filtrate returns denitration subsider;

(6) clear liquid on denitration subsider top is extracted out and is sent to denitration hypergravity machine, flows to denitration hypergravity machine together, carry out cyclic absorption denitration with after the sulfide reducing agent on-line mixing of supplementing.

Claims (1)

1. a method for hypergravity complexing ferrous flue-gas wet dust removal desulfurization denitration demercuration dearsenification integration, is characterized in that, comprise the following steps:
1) by temperature be 40 DEG C ~ 120 DEG C and send into dust-removal and desulfurizing hypergravity machine containing SOx, NOx, mercury, arsenic flue gas, the concentration being 0 DEG C ~ 40 DEG C with the temperature entering dust-removal and desulfurizing hypergravity machine is sulfide solution counter current contacting in dust-removal and desulfurizing hypergravity machine rotor packing layer of 0.01 ~ 4.0mol/L, dedusting, desulfurization, demercuration, dearsenification; Described sulfide is selected from vulcanized sodium, NaHS, ammonium sulfide, ammonium hydro sulfide, potassium sulfide or potassium bisulfide;
2) denitration hypergravity machine is entered with the reacted flue gas of sulfide solution from dust-removal and desulfurizing hypergravity machine gaseous phase outlet, be absorbent counter current contacting in denitration hypergravity machine rotor packing layer of 0 DEG C ~ 55 DEG C again with the temperature entering denitration hypergravity machine, reaction denitration, wherein, described absorbent contains complexing ferrous iron and sulfide reducing agent, the complexing agent of described complexing ferrous iron is selected from the mixture of ethylenediamine tetra-acetic acid and citric acid, N-(2-ethoxy) ethylenediamine-N, N', the mixture of N'-triacetic acid and citric acid, ethylenediamine tetra-acetic acid and N-(2-ethoxy) ethylenediamine-N, N', the mixture of the mixture of N'-triacetic acid or nitrilotriacetic acid and diethylene triamine pentacetic acid (DTPA), described sulfide reducing agent is selected from vulcanized sodium, NaHS, ammonium sulfide, ammonium hydro sulfide, potassium sulfide or potassium bisulfide, in described absorbent, total Fe concentration is 0.01mol/L ~ 0.5mol/L, the mol ratio of sulfide and total Fe is 3:1 ~ 5:1, the mol ratio of described complexing agent and total Fe is 1.02:1 ~ 2:1, described total Fe refers to Fe 2+and Fe 3+sum, reacted purified gas enters demister from denitration hypergravity machine gaseous phase outlet, enters exhaust system subsequently,
3) after compensator, enter desulfurization subsider from dust-removal and desulfurizing hypergravity machine liquid out, by sulphur wherein, insoluble sulphurizing salt, ash fall to bottom, after filter filters, reclaim solid, filtrate returns desulfurization subsider;
4) clear liquid on desulfurization subsider top is extracted out and is sent to dust-removal and desulfurizing hypergravity machine, flows to dust-removal and desulfurizing hypergravity machine together, carry out cyclic absorption desulfurization with after the sulfide on-line mixing of supplementing;
5) after compensator, enter denitration subsider from denitration hypergravity machine liquid out, by sulphur wherein, insoluble sulfuration salt settling to bottom, after filter filters, reclaim solid, filtrate returns denitration subsider;
6) clear liquid on denitration subsider top is extracted out and is sent to denitration hypergravity machine, flows to denitration hypergravity machine together, carry out cyclic absorption denitration with after the sulfide reducing agent on-line mixing of supplementing.
CN201310403655.9A 2013-09-06 2013-09-06 The method of hypergravity complexing ferrous flue-gas wet dust removal desulfurization denitration demercuration dearsenification integration CN103432877B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201310403655.9A CN103432877B (en) 2013-09-06 2013-09-06 The method of hypergravity complexing ferrous flue-gas wet dust removal desulfurization denitration demercuration dearsenification integration

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201310403655.9A CN103432877B (en) 2013-09-06 2013-09-06 The method of hypergravity complexing ferrous flue-gas wet dust removal desulfurization denitration demercuration dearsenification integration

Publications (2)

Publication Number Publication Date
CN103432877A CN103432877A (en) 2013-12-11
CN103432877B true CN103432877B (en) 2015-11-25

Family

ID=49686648

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201310403655.9A CN103432877B (en) 2013-09-06 2013-09-06 The method of hypergravity complexing ferrous flue-gas wet dust removal desulfurization denitration demercuration dearsenification integration

Country Status (1)

Country Link
CN (1) CN103432877B (en)

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103768910B (en) * 2014-01-16 2015-09-16 昆明理工大学 SO in a kind of flue gas during smelting 2with heavy metal synergistic purification method and device
CN105561747A (en) * 2014-11-10 2016-05-11 江苏庆峰国际环保工程有限公司 Combined removal process for flue gas in coal-fired boiler
CN106281521B (en) * 2015-05-20 2019-05-17 北京化工大学 A kind of hypergravity natural gas removal of mercury clarification system
CN105214455B (en) * 2015-09-17 2017-12-01 昆明理工大学 A kind of while denitration removing heavy-metal method
CN105233647B (en) * 2015-09-17 2017-09-08 昆明理工大学 A kind of method of ammonium sulfide solution desulphurization denitration
CN105311947A (en) * 2015-12-08 2016-02-10 济南乾坤环保设备有限公司 Boiler fume denitration and desulfuration dedusting device and process
CN106474905A (en) * 2016-12-29 2017-03-08 焦作和信冶金科技有限责任公司 A kind of calcining fume desulfurizing and dedusting technology

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS54101762A (en) * 1978-01-27 1979-08-10 Asahi Chem Ind Co Ltd Removing method for nitrogen oxides contained in exhaust gas
CN102151476A (en) * 2011-03-29 2011-08-17 武汉国力通化工环保科技有限公司 Method for removing hydrogen sulfide in gas phase through oxidization under high gravity field
CN102949926A (en) * 2012-11-16 2013-03-06 昆明理工大学 Method for recycling sulfur dioxide (SO2) and heavy metal in metallurgical gas
CN103055666A (en) * 2011-10-21 2013-04-24 北京化工大学 Method for removing nitric oxide in flue gas

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP3651918B2 (en) * 1993-10-25 2005-05-25 バブコック日立株式会社 Control method of wet flue gas desulfurization equipment

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS54101762A (en) * 1978-01-27 1979-08-10 Asahi Chem Ind Co Ltd Removing method for nitrogen oxides contained in exhaust gas
CN102151476A (en) * 2011-03-29 2011-08-17 武汉国力通化工环保科技有限公司 Method for removing hydrogen sulfide in gas phase through oxidization under high gravity field
CN103055666A (en) * 2011-10-21 2013-04-24 北京化工大学 Method for removing nitric oxide in flue gas
CN102949926A (en) * 2012-11-16 2013-03-06 昆明理工大学 Method for recycling sulfur dioxide (SO2) and heavy metal in metallurgical gas

Also Published As

Publication number Publication date
CN103432877A (en) 2013-12-11

Similar Documents

Publication Publication Date Title
US10159931B2 (en) Control of wet scrubber oxidation inhibitor and byproduct recovery
CA2622064C (en) Method of removing sulfur trioxide from a flue gas stream
CN102430318B (en) System for desulfurizing and denitrating active coke flue gas, and process method
CN101745305B (en) Method for removing various gaseous pollutants from smoke gas
CN101254394B (en) Sintering device flue gas multiple pollutant removing process and system thereof
CN100496672C (en) Wet flue gas desulfurizing and hydrargyrum-removing technology based on two-stage oxidation reaction and system thereof
CN102459833B (en) Combustion flue gas NOX treatment
CN101564640B (en) Combined removal method for contaminants from coal-fired flue gas and special purification reactor thereof
CN102512927B (en) Integrated flue gas desulfurizing and denitrating purification system and purification technology for same
Pandey et al. Flue gas desulfurization: physicochemical and biotechnological approaches
CN102936651B (en) A kind of method sintering simultaneous SO_2 and NO removal system and desulphurization denitration thereof
CN103495333B (en) A kind of for the claus tail-gas clean-up technique containing sulfur dioxide, hydrogen sulfide and organic sulfur
CN103212284A (en) Method and device for combined removal of nitric oxide and sulfide in flue gas
KR20150131197A (en) Method of oxidizing mercury in flue gas
CN103933838B (en) In coal, chlorine element circular utilizes the device and method realizing pollutant combined removal
CN102716648B (en) Method for automatically controlling desulphurization and denitration by flue gas based on pH value and ORP value and apparatus thereof
CN103239985B (en) Efficient fuel coal flue gas desulfurizing and hydrargyrum-removing method and device thereof
CN104226095A (en) Synchronous denitration process based on wet ammonia process flue gas desulfurization
CN100391579C (en) Method for desulfurizing waste gas and reutilizing sulfur source
CN103301749A (en) Method for simultaneously performing desulfurization and denitrification on smoke gas
CN103480272A (en) Dust-removing, denitration and desulfurization process and device for flue gas of glass kiln
US9387435B2 (en) Mercury sorbents
CN103480251B (en) System and method for performing desulfurization, denitration and demercuration to flue gas simultaneously
US9289720B2 (en) System and method for treating mercury in flue gas
CN105617858B (en) A kind of assembled smoke gas multi-pollutant collaboration advanced purification process

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C41 Transfer of patent application or patent right or utility model
TA01 Transfer of patent application right

Effective date of registration: 20151009

Address after: 430206, Hubei, East Lake hi tech Development Zone, 999, hi tech Avenue No., the Future City Longshan Innovation Park Phase 1, A5, North District, 4, 8, A units

Applicant after: Wuhan Glt Energy and Environmental Technology Co., Ltd.

Address before: 430056 Hubei city of Wuhan province Zhuankou economic and Technological Development Zone SMTH 22 building 3 unit 302 room

Applicant before: Yu Guoxian

C14 Grant of patent or utility model
GR01 Patent grant
C56 Change in the name or address of the patentee
CP01 Change in the name or title of a patent holder

Address after: 430206, Hubei, East Lake hi tech Development Zone, 999, hi tech Avenue No., the Future City Longshan Innovation Park Phase 1, A5, North District, 4, 8, A units

Patentee after: Wuhan GLT Energy and Environmental Technology Co., Ltd.

Address before: 430206, Hubei, East Lake hi tech Development Zone, 999, hi tech Avenue No., the Future City Longshan Innovation Park Phase 1, A5, North District, 4, 8, A units

Patentee before: Wuhan Glt Energy and Environmental Technology Co., Ltd.

CF01 Termination of patent right due to non-payment of annual fee
CF01 Termination of patent right due to non-payment of annual fee

Granted publication date: 20151125

Termination date: 20160906