CN206355802U - A kind of hydrogen peroxide method flue gas desulfurization processing system - Google Patents
A kind of hydrogen peroxide method flue gas desulfurization processing system Download PDFInfo
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- CN206355802U CN206355802U CN201621288438.5U CN201621288438U CN206355802U CN 206355802 U CN206355802 U CN 206355802U CN 201621288438 U CN201621288438 U CN 201621288438U CN 206355802 U CN206355802 U CN 206355802U
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Abstract
The utility model provides a kind of hydrogen peroxide method flue gas desulfurization processing system.The desulfurization process system includes the reactive absorption tower of four layers of design of single column, hydrogen peroxide holding vessel, circulating pump, circulating slot and chimney；Wherein the floor of reactive absorption tower four is that demisting floor is absorption tower first layer, circulation fluid room i.e. the absorption tower second layer, absorbed layer i.e. absorption tower third layer and the gas mixer chamber i.e. floor of absorption tower the 4th.Desulfurization process system architecture of the present utility model is simple, convenient operation and control, and its desulfuration efficiency is high；And processing system corollary equipment is few, without additionally increasing operating personnel, effectively save cost of investment, operating cost and floor space, more than 98% desulfuration efficiency can be realized, in the absence of the stifled tower problem of crystallization, its byproduct dilute sulfuric acid is not required to secondary operation, and cost recovery is low, three new waste products, and non-secondary pollution are not produced in whole production process.
Description
Technical field
The utility model belongs to flue gas desulfurization technique field, and in particular to a kind of hydrogen peroxide method flue gas desulfurization processing system
System.
Background technology
It is well known that oxysulfide and nitrogen oxides turn into China's Air Pollutants, and it is many with acid rain, haze etc.
The form of kind does great damage to ecological environment, greatly negative effect is caused to whole national economy, to the Working Life of people
Cause high risks.China sulfur dioxide (SO2) main source be the related work of the huge sulfuric acid market demand of China and part
The sulfur dioxide discharged in industry enterprise production accessory substance, is to be related to environment to protect to the sulfur dioxide progress processing in sulfuric acid tail gas
The big problem of shield and economic benefit, is also China SO2The emphasis of emission reduction.
Current China sulfuric acid industry is more for the method and processing system equipment of sulfuric acid tail gas desulfurization process, its method bag
Ammonia-acid process, ammonia process, sodium alkali, Citrate Buffer, limestone-gypsum method, activated coke method etc. are included, wherein most widely used
There are ammonia-acid process, limestone-gypsum method and activated coke method several.And from the point of view of the desulfurization process system and equipment of industrialization,
Have that floor space is big, operating cost is high, absorption tower is easily blocked, the defect such as desulfurizing byproduct is difficult to dispose；And secondary pollution is asked
The serious limestone-gypsum method of topic and its equipment still account for absolute leading position due to historical reasons.Although desulfurization technology passes through state
Inside and outside updates and engineering practice, and existing activated coke method desulfurization technology is quite ripe, particularly in western water shortage
Area, activated coke method desulfurization technology should be a kind of good selection.But this method contrasts new catalytic law technology, exist used
Activated coke is easy to wear, easily burns, lumps, high energy consumption during thermal regeneration, the problems such as operating cost is high.And ammonia-acid process desulfurization
There is NH_3 leakage, desulfurization degree not high, product thiamine process long flow path and complex operation, also association some ammonium sulfites in production,
Ammonium sulfite less stable itself, is irradiated or hits rear portion branch by sunlight and decompose generation SO2And CO2, form secondary pollution.
Number of patent application 201310371346.8, it is entitled " to be used for different flue gas activated coke high-efficiency energy-saving desulfurizings and purify system
The patent of invention of system and method ", the desulfurizing and purifying system includes the first absorption desulfurization section, the second absorption desulfurization section, activated coke
Regenerator section and activated coke conveying equipment；Although the cleaning system and its desulfurization degree of method are higher, there is floor space greatly, operation
Cost is high, the problem of activated coke is easy to wear.
Number of patent application 201420140181.3, the utility model patent of entitled " ammonia type flue gas desulfurizing apparatus ", it is tied
Structure includes flue, desulfurizing tower, ammonia circulation system and oxidative system.In the desulfurizer, sulfur dioxide reacts with ammoniacal liquor to be generated
Cigarette ammonium sulfate, then oxidized system oxidation be ammonium sulfate.There is oxidation not exclusively in the oxidative system, some sulfurous of meeting association
The shortcoming of sour ammonium, ammonium sulfite less stable itself is similarly subjected to sunlight irradiation or may can decompose generation SO after hitting2With
CO2, secondary pollution is formed, so as to further result in the vicious circle of environmental pollution.
The content of the invention
The purpose of this utility model exactly for it is above-mentioned the problems of in the prior art and not enough there is provided a kind of peroxide
Change hydrogen method flue gas desulfurization processing system.Reactive absorption tower is four layers of design of single column, whole processing system in the desulfurization process system
Complete equipment under unified central planning is fewer but better, without extra increase operating personnel, effectively save cost of investment, operating cost and floor space, energy
More than 98% desulfuration efficiency is realized, in the absence of the stifled tower problem of crystallization, three new waste products are not produced in production process, and without secondary
Pollution.
For achieving the above object, the utility model is realized using the technical scheme being made up of following technical measures
's.
A kind of hydrogen peroxide method flue gas desulfurization processing system described in the utility model, including reactive absorption tower, hydrogen peroxide
Holding vessel, conveyance conduit, circulating pump, circulating slot and chimney；Wherein, the reactive absorption tower is using four layers of design of single column：Four layers
It is absorption tower first layer for demisting layer, demisting floor is the absorption tower second layer close to circulation fluid room, and circulation fluid room is close to absorbed layer
Absorption tower third layer, absorbed layer close to gas mixer chamber be the 4th layer of absorption tower；The hydrogen peroxide holding vessel is placed in reaction and inhaled
Tower bottom left-external side is received, is connected by input channel with reactive absorption tower bottom gas mixer chamber, gas mixer chamber is inhaled with reaction
Circulating pump connection on the outside of tower lower right is received, circulating pump is connected with right outside circulating slot in the middle part of reactive absorption tower, and circulating slot connection is anti-
Answer circulation fluid room in absorption tower, the chimney is installed on the outside of reactive absorption top of tower, flue gas by after demisting layer through delivery pipe
Road is by smoke stack emission into air.
In the utility model such scheme, four layers of the single column of the reactive absorption tower is designed as large opening rate packed tower or sky
Tower.
In the utility model such scheme, the demisting layer is to be provided with demister in the first layer of absorption tower.
In the utility model such scheme, the circulation fluid room is to be provided with some dilution heat of sulfuric acid in the second layer of absorption tower
Shower nozzle.
Hydrogen peroxide method flue gas desulfurization processing system described in the utility model is using the control that PLC is programmable logic controller (PLC)
System processed is controlled, and control room is not required to set general surveillance equipment, and monitoring and the control of device are realized by PLC.
In desulfurization process system described in the utility model, the desulphurizing activated strong, reaction rate of hydrogen peroxide used is fast, titanium dioxide
The concentration of emission of sulphur is less than 200mg/m3Hereinafter, far below standard GB/T 26132-2010 requirement, desulfurization degree is up to 98%
More than, also there is higher removal efficiency to nitrogen oxides, and desulphurization denitration can be carried out simultaneously.In the desulfurization process system, by
In reactive absorption tower using four layers of design of single column, therefore desulfurization process system support equipment is fewer but better, without extra increase operation
Three new waste products are not produced in personnel, effectively save cost of investment, operating cost and floor space, whole production process, and
Non-secondary pollution.
The utility model has the advantage that compared with prior art and beneficial technique effect is as follows：
1st, a kind of hydrogen peroxide method flue gas desulfurization processing system described in the utility model is using four layers of design of single column, and this is anti-
Answer the recovery of absorption tower absorbing reaction and byproduct in a tower, corollary equipment is fewer but better, and workable, without volume
Outer increase operating personnel, effectively save cost of investment, operating cost and floor space.
2nd, taken off in a kind of hydrogen peroxide method flue gas desulfurization processing system described in the utility model, the desulfurization process system
Sulphur byproduct is dilute sulfuric acid, and the problem of tower is blocked up in crystallization is not present compared with conventional treatment systems.
3rd, absorption tower is filled out for large opening rate in a kind of hydrogen peroxide method flue gas desulfurization processing system described in the utility model
Expect tower or void tower, its SR is less than≤600Pa, therefore can save system dynamic consumption.
4th, in hydrogen peroxide method flue gas desulfurization processing system described in the utility model, produced dilute sulfuric acid is returned directly to
It is used to adjust acid concentration in reactive absorption tower, byproduct is not required to secondary operation, and cost recovery is substantially reduced；In whole production process
Three new waste products, thus non-secondary pollution, the typical cleaning desulfurization process system of category are not produced.
Brief description of the drawings
Fig. 1 is a kind of overall structure diagram of hydrogen peroxide method flue gas desulfurization processing system described in the utility model.
In figure, 1 reactive absorption tower, 2 demisting layers are absorption tower first layer, and 3 circulation fluid rooms are the absorption tower second layer, and 4 absorb
Layer is absorption tower third layer, and 5 gas mixer chambers are the 4th layer of absorption tower, 6 hydrogen peroxide holding vessels, 7 conveyance conduits, 8 demisters,
9 dilution heat of sulfuric acid shower nozzles, 10 circulating pumps, 11 circulating slots, 12 chimneys.
Embodiment
Below in conjunction with the accompanying drawings and the utility model is described in further detail by embodiment, but simultaneously unexpectedly
It is any restriction to the utility model protection domain that taste, which,.
A kind of hydrogen peroxide method flue gas desulfurization processing system described in the utility model, its structure are as shown in figure 1, including reaction
Absorption tower 1, hydrogen peroxide holding vessel 6, conveyance conduit 7, circulating pump 10, circulating slot 11 and chimney 12；Wherein, the reactive absorption
Tower 1 is using the design of four layers of single column, including its middle part demisting layer 2 i.e. absorption tower first layer, and demisting floor 2 is close to circulation fluid room in the middle part of it
The 3 i.e. absorption tower second layer, circulation fluid room 3 is absorption tower third layer close to its middle part absorbed layer 4, and absorbed layer 4 is close to its bottom gas
Body mixing chamber 5 is the 4th layer of absorption tower；The hydrogen peroxide holding vessel 6 is placed in outside the lower left side of reactive absorption tower 1, passes through conveying
Pipeline 7 is connected with the gas mixer chamber 5 of the bottom of reactive absorption tower 1, and gas mixer chamber 5 is through under conveyance conduit 7 and reactive absorption tower 1
The circulating pump 10 installed outside portion right side is connected, and circulating pump 10 is through following for being designed outside conveyance conduit 7 and the middle part of reactive absorption tower 1 right side
Annular groove 11 is connected, and it is molten that circulating slot 11 is connected to some dilute sulfuric acids installed in reactive absorption tower in circulation fluid room 3 through conveyance conduit 7
Set and installed on the outside of a demister 8, reactive absorption top of tower in chimney 12, reactive absorption tower in liquid shower nozzle 9, the demisting layer 2
Flue gas after demisting layer 2 through connecting the conveyance conduit of chimney by being emitted into air.
Embodiment 1
The present embodiment desulfurization process system architecture as described in Fig. 1 connects each instrument and equipment, utilizes the desulfurization process system
Operated according to following desulfurization treatment process step and the parameter；Whole operation process is FPGA control using PLC
The control system of device processed is controlled, and control room is not required to set general surveillance equipment, the monitoring of device and control by PLC come
Realize.
Following processing step scrubbing CO_2 is used using a kind of hydrogen peroxide method flue gas desulfurization processing system：
(1) sulfuric acid tail gas parameter is adjusted
Before sulfuric acid tail gas enters reactive absorption tower, sulfuric acid tail gas temperature is regulated, pressure, each parameter of oxygen content makes
Sulfuric acid tail gas meets desulfurization requirement；
(2) mixed gas is formed
The sulfuric acid tail gas that step (1) is regulated into parameter is passed through gas mixer chamber i.e. absorption tower the 4th in reactive absorption tower
Layer, the hydrogen peroxide in hydrogen peroxide holding vessel is sent into decompose after gas mixer chamber in reactive absorption tower by conveyance conduit and produced
Unboiled water and oxygen, the oxygen and sulfuric acid tail gas of generation are reacted in a mixed contact manner in reactive absorption tower in gas mixer chamber, and formation contains
There is the mixed gas of sulfur trioxide；
(3) sulfur dioxide is removed
Mixed gas through step (2) formation is the dilute sulfuric acid in the second layer of absorption tower with circulation fluid room in reactive absorption tower
Solution shower nozzle spray and lower dilution heat of sulfuric acid absorbed layer in reactive absorption tower to be absorption tower third layer mixing contact, after contact
Sulfuric acid tail gas be then dissolved in dilute sulfuric acid and fall into reactive absorption tower bottom, now sulfur dioxide is removed；The dilute sulfuric acid
Solution is to be produced through desulfurization process system, is conveyed again after the circulating slot being delivered to by circulating pump through conveyance conduit outside reactive absorption tower
To circulation fluid room；
(4) dilution heat of sulfuric acid is recycled
The dilution heat of sulfuric acid that step (3) is produced, drains into outside circulating pump through conveyance conduit from reactive absorption tower bottom and follows
In annular groove；Dilute sulfuric acid concentration in circulating slot is adjusted, after its concentration reaches 2.90%, circulating reflux is circulated into reactive absorption tower
The dilution heat of sulfuric acid of liquid room is sprayed through dilution heat of sulfuric acid shower nozzle again and absorbed layer is mixed in reactive absorption tower with mixed gas down
Contact；Above-mentioned steps (3) process of circulation, to reach the removal of sulfur dioxide；
(5) fume emission up to standard is into air
The sulfuric acid tail gas is absorption tower first layer by demisting layer in reactive absorption tower after the purification of step (1)-(4)
After the demister water removal of installation is dried, the conveyance conduit feeding cigarette of connection at the top of the reacted absorption tower of flue gas of discharge standard is reached
Chimney is emitted into air.
The content of sulfur dioxide of the present embodiment sulfuric acid tail gas air inlet is 1600mg/Nm3, regulation sulfuric acid tail gas temperature is 60
DEG C, admission pressure is 1500Pa, and oxygen content is 4%, and hydrogenperoxide steam generator concentration of absorbing used is 0.1%.
Reactive absorption tower parameter used is reactive absorption tower diameter D=4.8m packed tower, height H=15.5m；It is used
Circulating pump is Yang Cheng 30m, and flow is 300m3/ h 904L centrifugal pump of horizontal axis two (the using and the reserved)；Conveyance conduit used is selected
Fiberglass or stainless steel.
The present embodiment is as follows using the specific operation process and step of the desulfurization process system scrubbing CO_2：
(1) sulfuric acid tail gas parameter, is adjusted
The sulfuric acid tail gas for regulating each parameter is passed through the bottom gas mixing chamber 5 of reactive absorption tower 1 i.e. the 4th layer of absorption tower；
(2), mixed gas is formed
By its concentration being stored in hydrogen peroxide holding vessel 6 for 27.5% hydrogenperoxide steam generator absorbent through delivery pipe
Road 7 is delivered to the bottom gas mixing chamber 5 of reactive absorption tower 1, and decomposes generation water and oxygen, the sulfuric acid tail gas that step 1 is passed through with
Oxygen generates the mixed gas containing sulfur trioxide after the mixing and contacting reaction of gas mixer chamber 5；
(3) sulfur dioxide, is removed
Dilute sulfuric acid through step (2) mixed gas and the i.e. absorption tower second layer in circulation fluid room 3 in reactive absorption tower 1 is molten
Liquid shower nozzle 9 spray and under dilution heat of sulfuric acid the absorbed layer 4 of reactive absorption tower 1 i.e. absorption tower third layer mixing contact, after contact
Sulfuric acid tail gas be then dissolved in dilute sulfuric acid and fall into the bottom of reactive absorption tower 1, and contact after sulfuric acid tail gas with 1:40 volume ratios
It is dissolved in dilute sulfuric acid, now sulfur dioxide is removed；The dilution heat of sulfuric acid is to be produced through desulfurization process system, is inhaled by reaction
Receive after the circulating pump 10 outside tower bottom is delivered to the circulating slot 11 outside in the middle part of reactive absorption tower through conveyance conduit 7 again through conveyance conduit
It is delivered to circulation fluid room 3；
(4) dilution heat of sulfuric acid is recycled
By the dilution heat of sulfuric acid described in step (3), from the bottom of reactive absorption tower 1 through draining into circulating slot 11 outside circulating pump 10
It is interior；Dilute sulfuric acid concentration in circulating slot 11 is adjusted, after the regulation of its concentration is to 2.90%, circulating reflux is followed into reactive absorption tower 1
The dilution heat of sulfuric acid of ring liquid room 3 is sprayed and lower and mixed gas absorbed layer 4 in reactive absorption tower through dilution heat of sulfuric acid shower nozzle again
Mixing contact, circulate the process of above-mentioned steps 3, the sulfuric acid concentration of circulation fluid room 3 in reactive absorption tower is maintained in 20%, with up to
To the acid concentration for absorbing requirement；So as to reach the removal of sulfur dioxide；
(5) fume emission up to standard is into air
The sulfuric acid tail gas passes through demisting layer 2 i.e. absorption tower first layer in reactive absorption tower after the purification of step (1)-(4)
After the water removal of demister 8 of interior installation is dried, reach that the conveyance conduit of the reacted top of absorption tower 1 connection of flue gas of discharge standard is sent
Enter smoke stack emission into air.
When the utility model carries out desulphurization denitration operation by the desulfurization treatment process and desulfurization process system of embodiment 1,
Absorbent wherein used is 27.5% hydrogenperoxide steam generator, and the dilution heat of sulfuric acid concentration control is being not less than 2.90%, instead
It is that sulfuric acid concentration is maintained at 20%, sulfuric acid tail gas in 0.1%, absorbed layer to answer hydrogen peroxide ultimate density in the absorbed layer 4 of absorption tower 1
Intake air temperature is 60 DEG C, and pressure is 1500Pa, and sulfuric acid tail gas air inlet content of sulfur dioxide is 1600mg/Nm3.At desulphurization system
Sulfur dioxide concentration is less than 200mg/Nm after reason3, desulfurization degree is more than 98%.
Embodiment 2
Equally structure connects each instrument and equipment to the present embodiment as shown in Figure 1, its instrument equipment and operating process and
Step is same as Example 1, and the difference of embodiment 1 is, the sulfuric acid tail gas intake air temperature is 70 DEG C, reactive absorption tower
Hydrogenperoxide steam generator concentration of absorbing is that sulfuric acid concentration is maintained at 25% in 0.5%, absorbed layer in 1 absorbed layer 4, other ginsengs used
Number and all same of embodiment 1.Its sulfur dioxide concentration is less than 200mg/Nm after being handled through desulphurization system3, desulfurization degree is more than 98%.
Embodiment 3
Equally structure connects each instrument and equipment to the present embodiment as shown in Figure 1, its instrument equipment and operating process and
Step is same as Example 1, and difference is, the sulfuric acid tail gas intake air temperature is 80 DEG C, the absorbed layer 4 of reactive absorption tower 1
Middle hydrogenperoxide steam generator concentration of absorbing is that sulfuric acid concentration is maintained at 30% in 1%, absorbed layer 4.After being handled through desulphurization system its
Sulfur dioxide concentration is less than 200mg/Nm3, desulfurization degree is more than 98%.
Claims (4)
1. a kind of hydrogen peroxide method flue gas desulfurization processing system, it is characterised in that including reactive absorption tower (1), hydrogen peroxide storage
Tank (6), conveyance conduit (7), circulating pump (10), circulating slot (11) and chimney (12)；Wherein, the reactive absorption tower (1) is single
Four layers of tower：There is demisting layer (2) i.e. absorption tower first layer, demisting floor is the absorption tower second layer, circulation fluid room close to circulation fluid room (3)
Be absorption tower third layer close to absorbed layer (4), absorbed layer close to gas mixer chamber (5) be the 4th layer of absorption tower；The peroxidating
Storing hydrogen tank is placed in reactive absorption tower bottom left-external side, is connected by input channel (7) and reactive absorption tower bottom gas mixer chamber
Connect, gas mixer chamber is connected with circulating pump (10) on the outside of reactive absorption tower lower right, circulating pump and the right side in the middle part of reactive absorption tower are outer
Side circulating slot (11) is connected, and circulation fluid room in circulating slot coupled reaction absorption tower, the chimney (12) is installed on reactive absorption tower
Top outer, flue gas after demisting layer through conveyance conduit by being emitted into air.
2. a kind of hydrogen peroxide method flue gas desulfurization processing system according to claim 1, it is characterised in that the reactive absorption
Four layers of the single column of tower (1) is designed as large opening rate packed tower or void tower.
3. a kind of hydrogen peroxide method flue gas desulfurization processing system according to claim 1 or claim 2, it is characterised in that the demisting layer
(2) it is that demister (8) is installed in the first layer of absorption tower.
4. a kind of hydrogen peroxide method flue gas desulfurization processing system according to claim 1 or claim 2, it is characterised in that the circulation fluid
Room (3) is to be provided with some dilution heat of sulfuric acid shower nozzles (9) in the second layer of absorption tower.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201621288438.5U CN206355802U (en) | 2016-11-29 | 2016-11-29 | A kind of hydrogen peroxide method flue gas desulfurization processing system |
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| CN201621288438.5U CN206355802U (en) | 2016-11-29 | 2016-11-29 | A kind of hydrogen peroxide method flue gas desulfurization processing system |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107890763A (en) * | 2017-11-30 | 2018-04-10 | 成武县晨晖环保科技有限公司 | A kind of chlorinated exhaust absorption process for producing trichloro-acetic chloride |
| CN107899403A (en) * | 2017-11-30 | 2018-04-13 | 成武县晨晖环保科技有限公司 | Chloroethene acylating acid method produces the tail gas sulphur dioxide sulfur method of chloracetyl chloride |
| CN114634832A (en) * | 2022-03-11 | 2022-06-17 | 山西农业大学 | Biological denitrification device for biogas |
-
2016
- 2016-11-29 CN CN201621288438.5U patent/CN206355802U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107890763A (en) * | 2017-11-30 | 2018-04-10 | 成武县晨晖环保科技有限公司 | A kind of chlorinated exhaust absorption process for producing trichloro-acetic chloride |
| CN107899403A (en) * | 2017-11-30 | 2018-04-13 | 成武县晨晖环保科技有限公司 | Chloroethene acylating acid method produces the tail gas sulphur dioxide sulfur method of chloracetyl chloride |
| CN114634832A (en) * | 2022-03-11 | 2022-06-17 | 山西农业大学 | Biological denitrification device for biogas |
| CN114634832B (en) * | 2022-03-11 | 2023-01-13 | 山西农业大学 | Biological denitrification device for biogas |
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