CN207755960U - A kind of dual alkali scrubbing FGD process improvement system - Google Patents
A kind of dual alkali scrubbing FGD process improvement system Download PDFInfo
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Abstract
The utility model provides a kind of dual alkali scrubbing FGD process improvement system, including desulfurizing tower (3), oxidation pond (6), sedimentation basin (7), circulatory pool (8), the oxidation pond (6), sedimentation basin (7) and circulatory pool (8) are sequentially connected；Wherein, the system also includes pans (4), anaerobic reduction reactor (5) and homogeneous pond (11)；The doctor solution outlet of the desulfurizing tower (3) is connected by pipeline with the inlet of the pans (4), and the liquid outlet of pans (4) is connected by pipeline with the inlet of the anaerobic reduction reactor (5)；First liquid outlet of the anaerobic reduction reactor (5) is connected by pipeline with the inlet of the oxidation pond (6)；The homogeneous pond (11) is connected by pipeline with the inlet of the anaerobic reduction reactor (5), to provide carbon source for the sulfate reducing bacteria in anaerobic reduction reactor (5).
Description
Technical field
The utility model is related to a kind of dual alkali scrubbing FGD process to improve system, belong to desulfurizing industrial fume technical field
Background technology
The mankind manufacture the SO of discharge2The first big pollutant of atmospheric environment, be cause acid rain major pollutants it
One.Currently, more mature flue gas desulfurization technique is mostly wet desulfurizing process both at home and abroad, such as limestone/gypsum method, double alkali
Method, sodium alkali, ammonia process, magnesium processes etc..Wherein, limestone/gypsum method is applied most because desulfurization material cost is relatively low, but this method is deposited
The problems such as investing big, operating cost height and equipment corrosion and scaling, blocking.Other sulfur methods have desulfurization material (such as carbonic acid
Sodium or sodium hydroxide, ammonium hydroxide, magnesia) of high cost, source is restricted and there are different degrees of secondary pollution problems.
Sodalime double alkali method absorbs SO using soda ash2, absorbing liquid is regenerated with lime again, and regeneration product is oxidized to stone
Cream；The gypsum of generation is precipitated in sedimentation basin, and drains into filter press filtering outward transport；Absorbing liquid circulating and recovering desulfurization after regeneration.It is double
The absorber portion and oxidation regeneration section reaction equation of alkali process are as follows：
Absorber portion：
2Na2CO3+SO2+H2O→2NaHCO3+Na2SO3(1)；
2NaHCO3+SO2→Na2SO3+H2O+2CO2↑ (2)；
2NaOH+SO2→Na2SO3+H2O (3)；
Na2SO3+SO2+H2O→2NaHSO3(4)；
Wherein, formula (1) and formula (2) are that startup stage soda ash solution absorbs SO2Reactional equation；Formula (4) is operational process
Key reaction formula；Key reaction formula when formula (3) is regenerated liquid pH higher.
Regenerating oxidation section：
The biological treatment field of sulfate-containing wastewater has numerous studies and utilization, commonly uses sulfate reducing bacteria (SRB) connection
It closes sulfur-oxidizing bacteria (SOB) and handles sulfate wastewater.Sulfate reduction is S by reduction section SRB2, see below formula (8) and formula
(9), then oxidation panel SOB by S2It is oxidized to S0, see below formula (10)；Sulfate reducing bacteria and sulfide oxidation bacterium are easier to simultaneously
Culture, is easy to industrial applicability.
2HS-+O2→2S0+2OH-(10)；
Due to desulfurizing byproduct Na2SO4Presence seriously affected the quality of gypsum, therefore generally based on abandoning, become solid
It is useless；Additionally, due to Ca2+Presence, double alkali method desulfurizing tower and pipeline scale block also more typical, cause to run unsmooth, maintenance frequency
Rate increases；Normal operation needs constantly consumption desulfurizing agent lime.
In view of sodalime double alkali method there are the problem of, seriously affected the occupation rate of market of the technique, while existing double alkali
Method technique also urgently improves exploitation.
202366619 U of Chinese patent CN provide a kind of sulfur removal technology with desulfurization bacterium storage tank, flue gas pass through successively into
Gas storage tank, deduster, cooling tower enter desulfurizing tower, the circulation fluid counter current contacting progress desulfurization come with desulfurization storage tank, under desulfurizing tower
End is connected with desulfurization storage tank, and desulfurization bacterium storage tank is connected by water pump with spray system in tower.
But the technical solution is recycled using desulfurization bacterium solution as desulfurizing agent, sulfate can accumulate in system always and
It cannot be discharged；Coal-fired flue-gas amount is very big, is less applicable in into gas storage tank.
Chinese patent CN 101073745A disclose a kind of bamboo-carbon filler biological drip filtering tower removing sulfur dioxide in flue gas
Method, this method sulfur oxidizing bacterium is by the SO in flue gas2It is oxidized to sulfate, byproduct FeSO4；But the technology needs
Autogamy nutrient solution is as carbon source, economy unobvious；Flue gas is directly entered absorption tower simultaneously, is not suitable for processing industrial high temperature cigarette
Gas.
Therefore it provides a kind of dual alkali scrubbing FGD process modified technique and system have become the technology of this field urgent need to resolve
Problem.
Utility model content
The purpose of this utility model is to provide a kind of dual alkali scrubbing FGD process to improve system.
In order to achieve the above object, the utility model, which provides a kind of dual alkali scrubbing FGD process, improves system, including desulfurizing tower 3,
Oxidation pond 6, sedimentation basin 7, circulatory pool 8, the oxidation pond 6, sedimentation basin 7 and circulatory pool 8 are sequentially connected；Wherein, the system is also
Including pans 4, anaerobic reduction reactor 5 and homogeneous pond 11；
The doctor solution outlet of the desulfurizing tower 3 is connected by pipeline with the inlet of the pans 4, and pans 4 go out
Liquid mouth is connected by pipeline with the inlet of the anaerobic reduction reactor 5；First liquid outlet of the anaerobic reduction reactor 5 is logical
Pipeline is crossed with the inlet of the oxidation pond 6 to be connected；
The homogeneous pond 11 is connected by pipeline with the inlet of the anaerobic reduction reactor 5, with for anaerobic reduction it is anti-
The sulfate reducing bacteria in device 5 is answered to provide carbon source.
According to the utility model specific embodiment, it is preferable that it further includes dedusting that the dual alkali scrubbing FGD process, which improves system,
Device 1 and booster fan 2, the deduster 1 are connected via booster fan 2 with the smoke inlet of the desulfurizing tower 3 by pipeline.
According to the utility model specific embodiment, it is preferable that it further includes press filtration that the dual alkali scrubbing FGD process, which improves system,
Machine 10, the filter press 10 are connected by pipeline with the outlet of the elemental sulfur of the sedimentation basin 7 precipitation.
According to the utility model specific embodiment, in the system, it is preferable that the regenerated liquid of the circulatory pool 8
Outlet is connected via circulating pump 9 with the spraying layer of the desulfurizing tower 3 by pipeline.
Wherein, the desulfurizing tower 3 is the conventional equipment that this field uses, and is internally provided with spraying layer, demister, and institute
The top that demister is located at desulfurizing tower 3 is stated, spraying layer is located between the smoke inlet and demister of the desulfurizing tower 3.
According to the utility model specific embodiment, it is preferable that it further includes oxidation that the dual alkali scrubbing FGD process, which improves system,
Wind turbine 13, the oxidation fan 13 are connected with the gas access of the oxidation pond 6.
According to the utility model specific embodiment, in the dual alkali scrubbing FGD process improvement system, the oxidation pond 6
Bottom is disposed with aeration facility, is aerated by air blower.
According to the utility model specific embodiment, in the dual alkali scrubbing FGD process improvement system, it is preferable that described
Semi-soft floating stuffing is filled in oxidation pond 6, to increase biomass.Wherein, the semi-soft floating stuffing is commercially available routine
Substance.
According to the utility model specific embodiment, in the dual alkali scrubbing FGD process improvement system, it is preferable that described
6 bottom of oxidation pond is additionally provided with oxidation-reduction potential (ORP) on-line computing model.Wherein, the oxidation-reduction potential (ORP) is online
Monitor is conventional equipment.
Wherein, the utility model can control the dissolved oxygen in oxidation pond (DO) by controlling the aeration quantity of oxidation fan
With oxidation-reduction potential (ORP), to ensure S0Yield.
According to the utility model specific embodiment, in the dual alkali scrubbing FGD process improvement system, the sedimentation basin 7
Can be inclined plate, inclined-tube sedimentation tank.
According to the utility model specific embodiment, in the system, it is preferable that the anaerobic reduction reactor 5
Filter tower or Anaerobic upflow are dripped including anaerobism.
According to the utility model specific embodiment, in the system, it is preferable that when the anaerobic reduction reactor
5 for anaerobism drip filter tower when, the second liquid outlet of the anaerobic reduction reactor 5 is anti-via spray pump 12 and anaerobic reduction by pipeline
The spraying layer of device 5 is answered to be connected.Wherein, the purpose of setting spray pump 5 is circulated sprinkling, is carried with dripping the microorganism in filter tower for anaerobism
For nutrition, and then sulphate reducing and sulphite.Wherein, the anaerobism drop filter tower belongs to anaerobic internal circulation reactor and anaerobism
Sequencing batch reactor, Anaerobic upflow belong to anaerobism fixed bed reactors.
According to the utility model specific embodiment, in the system, anaerobism drips filter tower and Anaerobic upflow
Filler used is physics, chemical stability height, can keep the filler of higher biomass；Preferably, filler used includes porous
The combination of one or more of haydite, activated carbon, cascade ring, fibrous porous plastics and polypropylene plastics.Wherein, porous pottery
Grain, activated carbon, cascade ring, fibrous porous plastics and polypropylene plastics are the conventional substances that this field uses.
According to the utility model specific embodiment, in the system, it is preferable that the pans 4 are additionally provided with
Overflow port, the overflow port are connected by pipeline with the inlet of the oxidation pond 6.Wherein, which is arranged the overflow port
Purpose be：When pans liquid level superelevation, the doctor solution in pans can enter oxidation pond by the overflow port overflow, and
Anaerobic reduction reactor 5 need not be flowed through.
According to the utility model specific embodiment, in the dual alkali scrubbing FGD process improvement system, the anaerobism is also
Advantageous flora is grown in former reactor and oxidation pond respectively, wherein the dominant microflora grown in reduction reactor is SRB, oxygen
It is SOB to change the dominant microflora grown in pond.
According to the utility model specific embodiment, in the dual alkali scrubbing FGD process improvement system, the homogeneous pond
11 be to contain the good sanitary sewage of biodegradability, produce the equal of one or more of organic wastewater and sludge fermentation liquid mixed liquor
Matter pond；At this point, the homogeneous pond 11 can be hydrolysis acidification pool, the sanitary sewage, production organic wastewater and sludge fermentation liquid
In the hydrolysis acidification pool carbon source can be provided after anaerobic hydrolysis-acidification for the SRB in reduction reactor；And life used
Sewage, production organic wastewater and sludge fermentation liquid living are the conventional substances that this field uses；
Or the homogeneous pond 11 is to contain the combination of one or more of methanol, formic acid, ethyl alcohol, acetic acid and lactic acid waste liquid
Homogeneous pond.Methanol, formic acid, ethyl alcohol, acetic acid and the lactic acid waste liquid contained in homogeneous pond can directly be in reduction reactor
SRB provide carbon source.
Wherein, the biodegradability is also referred to as the biodegradability of waste water, i.e. Organic Pollutants in Wastewater is biodegradable
Complexity, be one of key property of waste water.In this application, work as BOD5/COD>It can consider waste water when 0.45
Biodegradability is good.
System described in the utility model can be adapted for a variety of different methods and carry out dual alkali scrubbing FGD process, in order into
One step illustrates the system of the utility model, and the utility model is additionally provided carries out double alkali using the system of the utility model
The method of method flue gas desulfurization, the described method comprises the following steps：
Absorption processing is carried out to flue gas, so that the SO in flue gas2It is converted into SO3 2-、SO4 2-, flue gas after being purified and
Contain SO3 2-、SO4 2-Doctor solution；Wherein, this method is further comprising the steps of：
(1) dissolved oxygen in the doctor solution is removed, solution A is obtained；
(2) under sulfate reducing bacteria (SRB) existence condition, the solution A is subjected to anaerobic reduction so that SO3 2-、SO4 2-
S is reduced to by SRB2-, and basicity (pH value 7-8.5) is generated, it obtains containing S2-Solution；
Wherein, step (2) further includes the operation that carbon source is provided for SRB；
(3) under sulfur-oxidizing bacteria (SOB) existence condition, described it will contain S2-Solution is aoxidized so that S2-It is aoxidized by SOB
For S0, and basicity (pH value 8-9) is generated, it obtains containing S0Doctor solution；
(4) recycling contains S0S in doctor solution0Precipitation, and obtain supernatant.
According to the utility model specific embodiment, which further includes being carried out to flue gas
Before absorption processing, it is dusted and is boosted operation.Wherein, the boosting numerical value can give when voltage loss designs
Setting, in specific embodiment of the present invention, which can be with the conventional Dual alkali technique institute of current this field
It is identical with boosting numerical value.
According to the utility model specific embodiment, which further includes by the supernatant
(doctor solution after regeneration) is recycled back to the operation as desulfurization spray liquid.
According to the utility model specific embodiment, in the dual alkali scrubbing FGD process improved method, the carbon source packet
Include the sanitary sewage, production that one or more of methanol, formic acid, ethyl alcohol, acetic acid and lactic acid waste liquid combine or biodegradability is good
One or more of organic wastewater and sludge fermentation liquid mixed liquor are through anaerobic hydrolysis-acidification products therefrom.
According to the utility model specific embodiment, in the dual alkali scrubbing FGD process improved method, step (2) is described
The temperature of anaerobic reduction is 25-50 DEG C (being more preferably 35-45 DEG C), pH value 7-8.5.
According to the utility model specific embodiment, in the dual alkali scrubbing FGD process improved method, step (3) oxidation
The oxidation-reduction potential of process is not higher than -90mV.Wherein, the utility model can be controlled by controlling the aeration quantity of oxidation fan
The height of the oxidation-reduction potential is made, and it is detected using oxidation-reduction potential on-line computing model.
According to the utility model specific embodiment, which can pass through the Dual alkali
Flue gas desulfurization improves system and realizes, specifically includes following steps：
Flue gas first passes around deduster dedusting, is then boosted by booster fan, enters desulfurizing tower from smoke inlet, in tower
SO in flue gas2It is SO by the absorbing liquid sorption enhanced of spray system3 2-、SO4 2-, the flue gas emission after desulfurizing and purifying；
Then doctor solution enters pans buffering, and the dissolved oxygen of doctor solution is because of oxidized portion SO in pans3 2-It exhausts；
Anaerobic reduction reactor is entered back into, in the reactor SO3 2-、SO4 2-It is reduced by a large amount of SRB in carrier biofilm
S2-, and basicity is generated, see formula (8)-formula (9)；
What reactor generated contains S2-Doctor solution enters oxidation pond, in oxidation pond, S2-S is aoxidized by SOB0, and basicity is generated,
See formula (10)；
Containing S0Doctor solution from flowing into sedimentation basin, S0The elemental sulfur precipitation of precipitation, generation is recycled by filter press press filtration, is sunk
Shallow lake pond supernatant flows into circulatory pool certainly；Doctor solution is regenerated because of the basicity elevation process of front in circulatory pool, after regeneration
Doctor solution be recycled to be used in desulfurizing tower, continue desulfurization.
Wherein, the total alkalinity in the dual alkali scrubbing FGD process improved method includes the HS in solution-、HCO3 -、CO3 2-、OH-
And S2-The basicity that equal basic substances generate.
The purpose of this utility model aim to solve the problem that during traditional dual alkali scrubbing FGD process there are the drawbacks of, such as fouling, stifled
Plug, by-product solid waste, sorbent consumption etc. provide a kind of dual alkali scrubbing FGD process modified technique and system, i.e.,：Using microbial method
The regenerator section and oxidation panel for substituting traditional dual alkali scrubbing FGD process, generate basicity, realize desulfurization regeneration and are back to desulfurization, make
SO2The elemental sulfur of Resource recovery while qualified discharge；Specifically：
Compared with existing dual alkali scrubbing FGD process process, dual alkali scrubbing FGD process improved method provided herein warp
SRB reduction and SOB oxidation process are crossed, basicity is generated instead of the desulfurizing agent quick lime or calcium hydroxide in Dual alkali technique, reduces fortune
Row cost；
There is no the generation of gypsum solid waste in modified technique provided herein, it can be more thoroughly by sulphur from doctor solution
Removal, and the byproduct elemental sulfur (not generating gypsum) of recyclable high value；
Modified technique provided herein can also combine different aerobe fermentation bacterium
The electron donor that SRB is restored in system, and then the stain disease that processing biodegradability can be cooperateed with good.
Dual alkali scrubbing FGD process provided by the utility model improves system and can also realize to existing double alkali method desulfurizing technology
Project is directly transformed, i.e.,：By the profits such as wind turbine, desulfurizing tower and the circulating pump of existing dual alkali scrubbing FGD process system, filter press
It is old, by Ca (OH)2Alkali liquid tank transforms pans into, transforms oxidation regeneration pond into oxidation pond, sedimentation basin, circulatory pool are reused, and increases newly
Homogeneous pond and anaerobic reactor；It so as to reducing cost of investment, cuts operating costs, and improved technique and is
System and can recycle by-product at non-secondary pollution.
Description of the drawings
Fig. 1 improves system structure diagram by the dual alkali scrubbing FGD process that the utility model embodiment 1 provides.
Main Reference label declaration：
1- dedusters；
2- booster fans；
3- desulfurizing towers；
4- pans；
5- anaerobic reduction reactors；
6- oxidation ponds；
7- sedimentation basins；
8- circulatory pools；
9- circulating pumps；
10- filter presses；
11- homogeneous pond；
12- spray pumps；
13- oxidation fans.
Specific implementation mode
The implementation process of the utility model and having for generation is described in detail below by way of specific embodiment and Figure of description
Beneficial effect, it is intended to help reader to more fully understand the essence and feature of the utility model, not as can practical range to this case
Restriction.
Embodiment 1
Present embodiments provide a kind of dual alkali scrubbing FGD process and improve system, the structural schematic diagram of the system as shown in Figure 1,
From figure 1 it appears that the system includes desulfurizing tower 3, oxidation pond 6, sedimentation basin 7, circulatory pool 8, the oxidation pond 6, sedimentation basin 7
And circulatory pool 8 is sequentially connected；Wherein, the system also includes pans 4, anaerobic reduction reactor (anaerobism drop filter tower) 5 and
Matter pond 11；
The doctor solution outlet of the desulfurizing tower 3 is connected by pipeline with the inlet of the pans 4, and pans 4 overflow
Head piece is connected by pipeline with the inlet of the oxidation pond 6, and the liquid outlet of pans 4 is anti-by pipeline and the anaerobic reduction
The inlet of device 5 is answered to be connected；The inlet that first liquid outlet of the anaerobic reduction reactor 5 passes through pipeline and the oxidation pond 6
It is connected；
Second liquid outlet of the anaerobic reduction reactor (anaerobism drop filter tower) 5 is by pipeline via spray pump 12 and anaerobism
The spraying layer of reduction reactor 5 is connected；
The homogeneous pond 11 is connected by pipeline with the inlet of the anaerobic reduction reactor 5, with for anaerobic reduction it is anti-
The sulfate reducing bacteria in device 5 is answered to provide carbon source；
It further includes deduster 1 and booster fan 2 that the dual alkali scrubbing FGD process, which improves system, and the deduster 1 passes through pipe
Road is connected via booster fan 2 with the smoke inlet of the desulfurizing tower 3；
It further includes filter press 10 that the dual alkali scrubbing FGD process, which improves system, which passes through pipeline and the precipitation
The elemental sulfur precipitation outlet in pond 7 is connected；
The regenerated liquid outlet of the circulatory pool 8 is connected via circulating pump 9 with the spraying layer of the desulfurizing tower 3 by pipeline；
It further includes oxidation fan 13 that the dual alkali scrubbing FGD process, which improves system, the oxidation fan 13 and the oxidation pond 6
Gas access be connected；
6 bottom of the oxidation pond is disposed with aeration facility, is aerated by air blower；
Semi-soft floating stuffing is filled in the oxidation pond 6, to increase biomass；
6 bottom of the oxidation pond is additionally provided with oxidation-reduction potential on-line computing model.
Embodiment 2
A kind of dual alkali scrubbing FGD process improved method is present embodiments provided, is the system provided using embodiment 1
It realizes, specifically includes following steps：
2 40t/h coal-burning boilers, flue gas flow 240000m3/ h, SO2Content is 600mg/Nm3, flue-gas temperature is
100-160 DEG C, in the present embodiment, when flue gas leaves desulfurizing tower, export SO2Content is 20mg/Nm3, desulfuration efficiency 97%；
Using Na2CO3As desulfurizing agent is started, the regeneration of desulfurizing agent is realized by microbial process, saves desulfurizing agent
CaO53kg/h；
Wherein, desulfurizing tower is using conventional spray column, a diameter of 4.6m, tower always a height of 30m, liquid-gas ratio 2-5L/m3, tower
Interior flow velocity is 2-4m/s, and the loop slurry residence time is 3-5min；
Intermediate tank volume is 10m3, anaerobic reduction reactor is bio-trickling filter, a diameter of 6m, a height of 6m, sprinkle density
For 2-25m3/(m2H), spray pump is variable frequency pump, and water pump frequency, corresponding sprinkle density are adjusted according to entrance sulphates content
Variation.
PH is between 7-8.5 in anaerobic reactor, between temperature range is 35-45 DEG C.
Oxidation pool size is 2 × 4m of Ф, and sedimentation basin is 3 × 3m of Ф, and circulatory pool is 3 × 2 × 2.5m；Homogeneous pond is hydrolysis acid
Change pond, tank depth 5.5m, pH value 6；Homogeneous pit level is adjustable, related to season and amount of sulfur contenting in smoke；
Desulfurizing tower entrance is equipped with SO2The circulating pump of on-Line Monitor Device, desulfurizing tower uses more or separate unit frequency conversion control
System, with desulfurizing tower entrance SO2Concentration is chain；The degree of oxidation of oxidation pond is monitored on-line by ORP, and ORP is exposed by oxidation fan
Tolerance or aeration time control；
Flue gas first passes around deduster dedusting, is then boosted by booster fan, enters desulfurizing tower from smoke inlet, in tower
SO in flue gas2It is SO by the absorbing liquid sorption enhanced of spray system3 2-、SO4 2-, the flue gas emission after desulfurizing and purifying；
Then doctor solution enters pans buffering, and the dissolved oxygen of doctor solution is because of oxidized portion SO in pans3 2-And it consumes
To the greatest extent；
Anaerobic reduction reactor is entered back into, in the reactor SO3 2-、SO4 2-It is reduced by a large amount of SRB in carrier biofilm
S2-, and generate basicity；
What reactor generated contains S2-Doctor solution enters oxidation pond, in oxidation pond, S2-S is aoxidized by SOB0, and generate basicity；
Containing S0Doctor solution from sedimentation basin is flowed into, stand so that S0The elemental sulfur precipitation of precipitation, generation passes through filter press press filtration
Recycling, sedimentation basin supernatant flow into circulatory pool certainly；Doctor solution is regenerated because of the basicity elevation process of front in circulatory pool,
Doctor solution after regeneration is recycled to be used in desulfurizing tower, continues desulfurization.
Embodiment 3
The present embodiment is transformed the double alkali method desulfurizing system of the heating boiler of existing 110t/h, and processing exhaust gas volumn is
270000m3/ h, SO2Content is 800mg/Nm3, flue-gas temperature is 140 DEG C, and desulfuration efficiency is 95% or more.Wherein, desulfurization Sopwith staff
Very little is 5 × 22m of Ф, and desulfurizing tower reuses, its pulping tank (2.5 × 3m of Ф) is used as pans；By regenerating oxidation pond (6.5 ×
4.6 × 3m) it is changed to oxidation pond, change small oxidation fan；Reuse sedimentation basin (6.5 × 4.8 × 3m) and plate and frame filter press；Reuse cycle
Pond (6.5 × 4.6 × 3m)；Newly-increased homogeneous pond, and using periphery ethanol production plant plant effluent as SRB carbon sources；Newly-increased anaerobism
Reduction reactor, using Anaerobic upflow, residence time 3-10h, according to entrance SO2Content adjusts.
Claims (10)
1. a kind of dual alkali scrubbing FGD process improves system, including desulfurizing tower (3), oxidation pond (6), sedimentation basin (7), circulatory pool (8),
The oxidation pond (6), sedimentation basin (7) and circulatory pool (8) are sequentially connected；It is characterized in that, the system also includes pans
(4), anaerobic reduction reactor (5) and homogeneous pond (11)；
The doctor solution outlet of the desulfurizing tower (3) is connected by pipeline with the inlet of the pans (4), pans (4)
Liquid outlet is connected by pipeline with the inlet of the anaerobic reduction reactor (5)；The first of the anaerobic reduction reactor (5) goes out
Liquid mouth is connected by pipeline with the inlet of the oxidation pond (6)；
The homogeneous pond (11) is connected by pipeline with the inlet of the anaerobic reduction reactor (5), with for anaerobic reduction it is anti-
The sulfate reducing bacteria in device (5) is answered to provide carbon source.
2. system according to claim 1, which is characterized in that the system further includes deduster (1) and booster fan (2),
The deduster (1) is connected via booster fan (2) with the smoke inlet of the desulfurizing tower (3) by pipeline；
The system further includes filter press (10), which is settled out by the elemental sulfur of pipeline and the sedimentation basin (7)
Mouth is connected.
3. system according to claim 1, which is characterized in that the regenerated liquid outlet of the circulatory pool (8) is passed through by pipeline
It is connected with the spraying layer of the desulfurizing tower (3) by circulating pump (9).
4. system according to claim 1, which is characterized in that the system further includes oxidation fan (13), the oxidation fan
(13) it is connected with the gas access of the oxidation pond (6).
5. system according to claim 1, which is characterized in that the anaerobic reduction reactor (5) includes anaerobism drop filter tower
Or Anaerobic upflow.
6. system according to claim 5, which is characterized in that oxygen drips filler used in filter tower and Anaerobic upflow and includes
The combination of one or more of porous ceramic grain, activated carbon, cascade ring, fibrous porous plastics and polypropylene plastics.
7. system according to claim 5 or 6, which is characterized in that when the anaerobic reduction reactor (5) is anaerobism drop filter
When tower, the second liquid outlet of the anaerobic reduction reactor (5) is by pipeline via spray pump (12) and anaerobic reduction reactor (5)
Spraying layer be connected.
8. system according to claim 1, which is characterized in that the pans (4) are additionally provided with overflow port, the overflow port
It is connected with the inlet of the oxidation pond (6) by pipeline.
9. system according to claim 1, which is characterized in that be filled with semi-soft floating stuffing in the oxidation pond (6).
10. the system according to claim 1 or 9, which is characterized in that oxidation pond (6) bottom is additionally provided with oxidation also
Former current potential on-line computing model.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110801727A (en) * | 2019-12-03 | 2020-02-18 | 山东默锐环境产业股份有限公司 | Scale-free zero-discharge wet desulfurization device and desulfurization method |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110801727A (en) * | 2019-12-03 | 2020-02-18 | 山东默锐环境产业股份有限公司 | Scale-free zero-discharge wet desulfurization device and desulfurization method |
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