CN102091519A - Double-groove wet-process flue gas desulfuration device and method operating on basis of two pH values - Google Patents
Double-groove wet-process flue gas desulfuration device and method operating on basis of two pH values Download PDFInfo
- Publication number
- CN102091519A CN102091519A CN 201010608773 CN201010608773A CN102091519A CN 102091519 A CN102091519 A CN 102091519A CN 201010608773 CN201010608773 CN 201010608773 CN 201010608773 A CN201010608773 A CN 201010608773A CN 102091519 A CN102091519 A CN 102091519A
- Authority
- CN
- China
- Prior art keywords
- oxidation
- flue gas
- slurries
- absorption tower
- slurry
- Prior art date
- Legal status (The legal status 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 status listed.)
- Pending
Links
Images
Landscapes
- Treating Waste Gases (AREA)
Abstract
The invention discloses a double-groove wet-process flue gas desulfuration device and a double-groove wet-process flue gas desulfuration method operating on the basis of two pH values, which relate to a flue gas desulfuration device and a flue gas desulfuration method. The aim of the invention is to remove SO2 from the flue gas under a high pH value condition by using desulfurating spray slurry and to dissolve limestone and oxidize calcium sulfite under a low pH value condition so as to improve desulfuration efficiency and quality of gypsum and reduce limestone consumption, investment and operation cost. In the invention, a circulating oxidization tank at the bottom of an absorption tower is divided into two parts, an oxidation pond receives desulfurizating slurry flowing out from a desulfurization tower, the oxidation pond operates in a pH range from 4.0 to 5.5, and in the oxidation pond, sulfite ions are oxidized, and byproduct of desulfuration is led out from the oxidation pond; and fresh limestone slurry is added into a circulating pond, the circulating pond operates in a pH range from 6 to 6.5, and slurry is led from the circulating pound into the absorption tower to be sprayed for deselfuration. The device and the method contribute to improving quality of gypsum, desulfuration efficiency, reducing limestone consumption and lowering investment and operation cost, and are suitable for flue gas desulfuration when sulfur coal is burnt or different kinds of fire coal are burnt.
Description
Technical field
The present invention relates to a kind of flue gas desulfur device and fume desulphurization method, particularly relate to a kind of dual grooved wet flue gas desulfurizer and method, belong to industrial waste gas purifying environmental protection field based on two pH value operations.
Background technology
Wet process of FGD be use in the world at most at present, the most effective sulfur removal technology.In the limestone wet-process flue gas desulfurization technique, existing wet desulfuration tower integrates original cooling tower, absorption tower, oxidizing tower, and all chemical processes are all finished in a tower.In the wet process of FGD process, desulfurization slurry pH value is a very important parameter that influences.In the sweetening process, the oxidation of the dissolving of lime stone, sulfurous calcium is adapted at carrying out under the low pH, and high pH value helps SO
2Absorption, be the above-mentioned contradiction of compromising, existing desulfurizing tower loop slurry must move under the environment of pH value about 5.5, the result makes the quality of system's desulfuration efficiency and gypsum descend, the consumption of lime stone increases.For some coal-burning boilers, particularly when using sulphur coal, realize flue gas desulfurization, this problem is more outstanding, even the system that makes is difficult to meet the demands.
How can guarantee the quality of high desulfurization efficiency and desulfurizing byproduct gypsum simultaneously, and reduce investment and operating cost as far as possible, this solves the contradiction of bringing owing to the required pH value of desulfurizing tower loop slurry to a certain extent with regard to needs.
Overcome though the problems referred to above have been designed some devices both at home and abroad, also there are some problems in these devices at present.As the two circulation wet fuel gas desulfurizing technologies of the Nore of the U.S., domestic applications (patent) number is that 200620200307.7 " double circulation loop process for flue gas desulfurization by limestone/lime-gypsum wet device " and application (patent) number are 200720023289.4 " cross-flow pair circulation wet flue gas desulfurizers in the flue ", though adopt two pH value operational systems, but do not adopt oxidation for high pH value section, adopting the solid formation main body is the slurries circulation desulfurization of CaSO3, is easy to generate the scale problems that causes owing to autoxidation; The sprayed slurry of above-mentioned patent not all is to carry out desulfurization under high pH value, and desulfuration efficiency can further improve.Above-mentioned patent is moved for satisfying two pH values simultaneously, the double circulation loop system complex of employing, and the absorption tower inner member increases, and investment increases.
Summary of the invention
The purpose of this invention is to provide a kind of dual grooved wet flue gas desulfurizer and method, so that the desulfurization sprayed slurry removes the SO in the flue gas under high pH value based on two pH value operations
2, under low pH value, carry out the dissolving of lime stone and the oxidation of calcium sulfite, and then improve desulfuration efficiency, gypsum quality, reduce the consumption of lime stone, and reduce and invest and operating cost.
The present invention solves the problems of the technologies described above the technical scheme of taking to be:
Dual grooved wet flue gas desulfurizer based on two pH value operations of the present invention comprises absorption tower body, demister, spraying layer and circulating pump, demister, spraying layer from top to bottom are arranged in the upper part of body of absorption tower, the lower end sidewall of absorption tower body is provided with former smoke inlet, and the upper end sidewall of absorption tower body is provided with clean exhanst gas outlet; Described desulfurizer also comprises oxidation trough, circulating slot and loop slurry return pipe, and oxidation trough and circulating slot are arranged on the below of absorption tower body, and the upper end of the upper end of oxidation trough and circulating slot is communicated with; The absorption tower body is communicated with oxidation trough by the loop slurry return pipe; Oxidation trough is provided with the gypsum slurries outlet, and oxidation trough is provided with the oxidation air inlet; Circulating slot is provided with the lime stone slurry inlet; Circulating pump is used for that the loop slurry in the circulating slot (calcium-based slurries) is evacuated to the spraying layer place and advances atomizing.
It is as follows to utilize above-mentioned desulfurizer to carry out the process of wet process of FGD:
Step 1, the pending former flue gas of boiler enter in the body of absorption tower from the absorption tower body former smoke inlet in bottom (gas approach), by circulating pump (recycle slurry liquid pump) calcium-based slurries being evacuated to spraying layer from circulating slot simultaneously atomizes, calcium-based slurries drop after the atomizing flows downward and contact with the pending flue gas adverse current that upwards flows and carries out desulfurization, and the flue gas after the desulfurization continues upwards to flow after the demister demist from the clean exhanst gas outlet outflow of desulfurizing tower bodies top;
Collect by the conical hopper of body bottom, absorption tower after step 2, absorption tower body spray atomization slurry and the flue gas contact desulfuriation, and be incorporated into below the oxidation trough liquid level with the loop slurry return pipe; In the oxidation trough the HSO that accepts in the desulfurization slurry to be contained
3 -Be blown into the oxidation air institute oxidation in the slurries by the oxidation air inlet; By the jacking-type agitator slurries in the oxidation trough are stirred; Taking out the part slurries simultaneously in the oxidation trough effluxes and enters conventional gypsum dehydration system and carry out liquid-solid separation, solid formation after the separation effluxes as desulfurizing byproduct, liquid phase thing after the separation returns in the oxidation trough, and the pH value of slurries remains between the 4.0-5.5 in the oxidation trough;
Contained calcium sulfite passes through the central dividing plate overflow to circulating slot through the slurries of fully oxidation in the desulfurization slurry of accepting in step 3, the oxidation trough; In circulating slot, replenish lime stone slurry,, make the interior slurry pH value of circulating slot rise between the 6.0-6.5 by the dissolving of lime stone slurry; And the slurries in the circulating slot are stirred by the jacking-type agitator;
Slurries are beaten to spraying layer by circulating pump and are carried out desulfurization in the step 4, circulating slot, being atomized into drop under the spraying layer nozzle act flows to the bottom, absorption tower, with flue gas adverse current contact desulfuriation, the slurries after the desulfurization are collected by the loop slurry return pipe through the conical hopper of desulfurizing tower bottom and are introduced in the oxidation trough in the flow process.
The invention has the beneficial effects as follows:
The present invention is a kind of flue gas desulfur device that the function decoupling zero is set based on pH value step, after the present invention is primarily aimed at cooling tower, absorption tower, the unification of oxidizing tower three towers, all chemical processes are all finished in a tower, during the operation of the single pH value of desulphurization system environment, the quality of system's desulfuration efficiency and gypsum all descends to some extent, and the problem that the consumption of lime stone also increases to some extent proposes.After absorption tower bottom cycle oxidation trough carried out the branch groove, absorbed SO
2Slurries and the lime stone slurry that newly advances no longer mix, the pH value of slurries reduces in the oxidation trough, the oxidation rate of sulfite ion is accelerated, oxidation is more thorough, the dissolution velocity of low simultaneously pH value quickening lime stone.CaCO in the gypsum like this
3, CaSO
3Content reduce, improved the grade of gypsum; Ororrhea flows to charging spout in the oxidation trough, add lime stone and make the pH value rising of slurries in charging spout, and circulated sprinkling is to the absorption tower, thereby make the absorption tower sprayed slurry move than under the higher pH.Under the higher condition of absorption tower sprayed slurry pH value, under identical spray flux, can improve desulfurization degree; When guaranteeing identical desulfurization degree, can reduce spraying layer, reduce tower height, reduce cost, the power consumption of circulating pump and blower fan can reduce simultaneously, and the spray loop slurry is the fully gypsum slurries that contains small amount of limestone of oxidation of calcium sulfite, has solved desulphurization system fouling blockage problem, and security of system stability is high.The present invention is applicable to coal-burning boiler, particularly when using sulphur coal, needs to guarantee the quality of high desulfurization efficiency and gypsum, and needs to reduce the flue-gas desulfurizing engineering project of investment and operating cost as far as possible.
The loop slurry of this patent desulphurization system be contain a small amount of desulfurizing agent lime stone and calcium sulfite through fully being oxidized to the slurries of gypsum, the degree of supersaturation of system's gypsum can be controlled in below the critical degree of supersaturation that produces fouling, solve the scale problems of the two pH value operational systems of double circulation loop, solved the security of operation stability problem of system; And the slurries of all spraying layer sprays of desulphurization system are the high pH slurries in the circulatory pool, with respect to the two pH value operational systems of double circulation loop, are more conducive to the raising of desulfuration efficiency.This method is for satisfying two pH value operations, and the single cycle circuit system of employing is simple, and the absorption tower inner member does not increase, and has reduced investment.
The present invention has realized according to function division, satisfies the optimal design of difference in functionality in different pH values.When system can satisfy the desulfurization requirement, can suitably reduce the pH value in the oxidation trough, improve the quality of gypsum.When the boiler load increasing, or the sulfur content in fuel increase, in the time of can not satisfying the desulfurization requirement, can suitably improve the pH value in the circulating slot, improve desulfurization degree, the load adaptability of desulphurization system is strong, can satisfy the demand of different coal-fired sulfur-bearings, be particularly suitable for the changeable ruuning situation of China's boiler fired coal coal.
Therefore, after the present invention has eliminated cooling tower, absorption tower, the unification of oxidizing tower three towers, during the operation of the single pH value of desulphurization system environment, the quality of system's desulfuration efficiency and gypsum all descends to some extent, the problem that the consumption of lime stone also increases to some extent, and overcome the high pH target phase of two in the past circulations, be CaSO because loop-body adopts the solid formation main body
3The slurries circulation desulfurization, be easy to generate the scale problems that produces owing to autoxidation.
Description of drawings
Fig. 1 is the structural representation of wet desulphurization device of the present invention, and Fig. 2 is the structural representation (containing two absorption tower bodies) of wet desulphurization device described in the embodiment of the invention.
The specific embodiment
The specific embodiment one: as shown in Figure 1, the described dual grooved wet flue gas desulfurizer based on two pH value operations of present embodiment comprises absorption tower body 15, demister 2, spraying layer 3 and circulating pump 13, demister 2, spraying layer 3 from top to bottom are arranged in the top of absorption tower body 15, the lower end sidewall of absorption tower body 15 is provided with former smoke inlet 4, and the upper end sidewall of absorption tower body 15 is provided with clean exhanst gas outlet 1; It is characterized in that: described desulfurizer also comprises oxidation trough 6, circulating slot 10 and loop slurry return pipe 14, and oxidation trough 6 and circulating slot 10 are arranged on the below of absorption tower body 15, and the upper end of the upper end of oxidation trough 6 and circulating slot 10 is communicated with; Absorption tower body 15 is communicated with oxidation trough 6 by loop slurry return pipe 14; Oxidation trough 6 is provided with gypsum slurries outlet 7, and oxidation trough 6 is provided with oxidation air inlet 8; Circulating slot 10 is provided with lime stone slurry inlet 9; Circulating pump 13 is used for that the loop slurry (calcium-based slurries) in the circulating slot 10 is evacuated to spraying layer 3 places and advances atomizing.
Propose the corrective measure of cyclic oxidation groove, absorption tower bottom cycle oxidation trough is divided into two parts, the desulfurization slurry that a part is accepted outflow in the desulfurizing tower carries out oxidation at this sulfite ion, and from then on the desulfuration byproduct gypsum draws, and is called oxidation trough; And another part adds fresh lime stone slurry, and from then on slurries are introduced to spray in the absorption tower and carried out desulfurization, are called circulating slot.By this measure, make desulphurization system under two pH value environment, move.
With the cyclic oxidation groove of absorption tower bottom separately, can solve the contradictory problems of desulfurization degree and gypsum quality on certain degree.The pH value of slurries is far below pH value in the circulating slot in the oxidation trough, makes can keep than higher gypsum quality in the oxidation trough; Simultaneously, high circulating slot slurry pH value makes that slurry pH value improves in the absorption tower, and system's desulfurization degree is higher.When system can satisfy the desulfurization requirement, can suitably reduce the pH value in the charging spout, improve the quality of gypsum.When the boiler load increasing, or the sulfur content in fuel increase, in the time of can not satisfying the desulfurization requirement, can suitably improve the pH value in the charging spout, improve desulfurization degree, consider that from gypsum quality aspect the interior slurry pH value of circulating slot should be lower than 6.5.
The specific embodiment two: as shown in Figure 1, the described oxidation trough 6 of present embodiment, circulating slot 10 are to be made of cuboid pond body 17 and the dividing plates 11 that are arranged in the cuboid pond body 17, dividing plate 11 is divided into two parts as oxidation trough 6 and circulating slot 10 with the inner chamber of cuboid pond body 17 along its length direction, and the height of dividing plate 11 is lower than the height of cuboid pond body 17, and oxidation trough 6 and circulating slot 10 are connected.The design of employing cuboid, each pond top design jacking-type agitator has reduced the trouble point that conventional absorption tower side-feeding mixer is prone to fault.Between circulating slot 10 (circulatory pool) and oxidation trough 6 (oxidation pond) dividing plate 11 is set, contained calcium sulfite passes through the central dividing plate overflow to circulating slot through the slurries of fully oxidation in the desulfurization slurry of accepting in the oxidation pond.Other composition and annexation are identical with the specific embodiment one.
The specific embodiment three: as shown in Figure 1, the described desulfurizer of present embodiment also comprises two jacking-type agitators 5, and a jacking-type agitator 5 respectively is set in described oxidation trough 6 and the circulating slot 10; Loop slurry return pipe 14 liquid outlets are arranged at below oxidation pond 6 liquid levels, the top of jacking-type agitator 5.Other composition and annexation are identical with the specific embodiment one.
The specific embodiment four: as shown in Figure 1, the described desulfurizer of present embodiment also comprises conical hopper 16, and described conical hopper 16 is arranged in the bottom of absorption tower body 15 and conical hopper 16 liquid outlets are connected with loop slurry return pipe 14.Other composition and annexation are identical with the specific embodiment one, two or three.
The specific embodiment five: as shown in Figure 1, the described process of utilizing above-mentioned desulfurizer to carry out wet flue gas desulfurization method of present embodiment is as follows:
Step 1, the pending former flue gas of boiler enter in the absorption tower body 15 from the former smoke inlets 4 in absorption tower body 15 bottoms (gas approach), by circulating pump 13 (recycle slurry liquid pump) calcium-based slurries being evacuated to spraying layer 3 from circulating slot 10 simultaneously atomizes, calcium-based slurries drop after the atomizing flows downward and contact with the pending flue gas adverse current that upwards flows and carries out desulfurization, and the flue gas after the desulfurization continues upwards to flow after demister 2 demists from clean exhanst gas outlet 1 outflow of desulfurizing tower bodies top;
Collect by the conical hopper 16 of body bottom, absorption tower after step 2, absorption tower body 15 spray atomization slurries and the flue gas contact desulfuriation, and be incorporated into below oxidation trough 6 liquid levels with loop slurry return pipe 14; In the oxidation trough 6 the HSO that accepts in the desulfurization slurry to be contained
3 -By the 8 oxidation air institute oxidations that are blown in the slurries that enter the mouth by oxidation air; Stir by the slurries in 5 pairs of oxidation troughs of jacking-type agitator 6; Taking out the part slurries simultaneously in the oxidation trough 6 effluxes and enters conventional gypsum dehydration system and carry out liquid-solid separation, solid formation after the separation effluxes as desulfurizing byproduct, liquid phase thing after the separation returns in the oxidation trough 6, and the pH value of slurries remains between the 4.0-5.5 in the oxidation trough 6;
Contained calcium sulfite passes through central dividing plate 11 overflows to circulating slot 10 through the slurries of fully oxidation in the desulfurization slurry of accepting in step 3, the oxidation trough 6; In circulating slot 10, replenish lime stone slurry,, make circulating slot 10 interior slurry pH values rise between the 6.0-6.5 by the dissolving of lime stone slurry; And stir by the slurries in 5 pairs of circulating slots of jacking-type agitator 10;
Slurries carry out desulfurization by 13 dozens of circulating pumps to spraying layer again in the step 4, circulating slot 10, being atomized into drop under the spraying layer nozzle act flows to the bottom, absorption tower, with flue gas adverse current contact desulfuriation, the slurries after the desulfurization are collected by loop slurry return pipe 14 through the conical hopper 16 of desulfurizing tower bottom and are introduced in the oxidation troughs 6 in the flow process.
Collect by the conical hopper of body bottom, absorption tower after absorption tower spray atomization slurry and the flue gas contact desulfuriation, and be incorporated into below the oxidation pond liquid level with pipe, oxidation pond agitator top, this design makes that on the one hand the flue gas that enters the absorption tower has the effect of water seal, on the other hand, enter from the absorption tower slurries of agitator can be rapidly effect by agitator be distributed to oxidation pond, be beneficial to the carrying out of physical-chemical reaction process in the groove, and after having avoided entering oxidation pond from the slurries that the absorption tower flows into the direct overflow of short circuit to circulatory pool.
The specific embodiment six: as shown in Figure 1, in the present embodiment, loop slurry time of staying in oxidation pond remains on 2.5-5min, and loop slurry time of staying in circulatory pool remains at 1-2min.During design, draw above-mentioned parameter according to coal-fired sulfur content.Other composition and annexation are identical with the specific embodiment five.
Embodiment:
Embodiment 1: as shown in Figure 1:
The pending former flue gas of boiler enters absorption tower 15 from absorption tower body bottom inlet flue 4, by recycle slurry liquid pump 13 calcium-based slurries being evacuated to spraying layer 3 from circulatory pool simultaneously atomizes, calcium-based slurries drop after the atomizing flows downward and contact with the pending flue gas adverse current that upwards flows and carries out desulfurization, and the flue gas after the desulfurization continues upwards to flow after demister 2 demists from clean exhanst gas outlet 1 outflow of desulfurizing tower bodies top;
Collect by the conical hopper of body bottom, absorption tower after absorption tower 15 spray atomization slurries and the flue gas contact desulfuriation, and be incorporated into below oxidation pond 6 liquid levels with pipe 14; In the oxidation pond 6 the HSO that accepts in the desulfurization slurry to be contained
3 -Be blown into 8 oxidations of oxidation air in the slurries; Oxidation pond 6 is provided with jacking-type agitator 5; Take out the part slurries simultaneously in the oxidation pond 6 and efflux and enter conventional gypsum dehydration system and carry out liquid-solid separation, the solid formation after the separation effluxes as desulfurizing byproduct, and the liquid phase thing after the separation returns oxidation pond 6.The pH value of slurries remains between the 4.0-5.5 naturally in oxidation pond 6.
Contained calcium sulfite passes through central dividing plate 11 overflows to circulating slot 10 through the slurries of fully oxidation in the desulfurization slurry of accepting in the oxidation pond 6; In circulating slot 10, replenish lime stone slurry,, make the interior slurry pH value of circulating slot rise between the 6.0-6.5 by the dissolving of lime stone slurry; In the circulatory pool 10 slurries again by 13 dozens of circulating pumps to spraying layer.Jacking-type agitator 5 is set on circulatory pool.
Circulating pump 13 is beaten slurries to spraying layer 3 from circulatory pool, being atomized into drop under the spraying layer nozzle act flows toward the bottom, absorption tower, with flue gas adverse current contact desulfuriation, the slurries after the desulfurization are collected by pipeline 14 through the conical hopper of desulfurizing tower bottom and are introduced oxidation ponds 6 in the flow process.
Embodiment 2: as shown in Figure 2:
Realize flue gas desulfurization for many boilers, every pending former flue gas of boiler enters absorption tower 15 from absorption tower body bottom inlet flue 1 separately respectively, by recycle slurry liquid pump 13 calcium-based slurries being evacuated to spraying layer 3 from circulatory pool simultaneously atomizes, calcium-based slurries drop after the atomizing flows downward and contact with the pending flue gas adverse current that upwards flows and carries out desulfurization, and the flue gas after the desulfurization continues upwards to flow after demister 2 demists from clean exhanst gas outlet 1 outflow of desulfurizing tower bodies top;
Collect by the conical hopper of body bottom, absorption tower after each absorption tower 15 spray atomization slurry and the flue gas contact desulfuriation, after the slurries that collect on each absorption tower conflux by pipeline, be incorporated into below public oxidation pond 6 liquid levels with pipe 14; In the oxidation pond 6 the HSO that accepts in the desulfurization slurry to be contained
3 -Be blown into 8 oxidations of oxidation air in the slurries; Oxidation pond 6 is provided with jacking-type agitator 5; Take out the part slurries simultaneously in the oxidation pond 6 and efflux and enter conventional gypsum dehydration system and carry out liquid-solid separation, the solid formation after the separation effluxes as desulfurizing byproduct, and the liquid phase thing after the separation returns oxidation pond 6.The pH value of slurries remains between the 4.0-5.0 naturally in oxidation pond 6.
Contained calcium sulfite passes through central dividing plate 11 overflows to public circulating slot 10 through the slurries of fully oxidation in the desulfurization slurry of accepting in the oxidation pond 6; In circulating slot 10, replenish lime stone slurry,, make the interior slurry pH value of circulating slot rise between the 6.0-6.5 by the dissolving of lime stone slurry; In the circulatory pool 10 slurries again 13 dozens of circulating pumps by corresponding each absorption tower to spraying layer.Jacking-type agitator 5 is set on circulatory pool.
The circulating pump 13 on corresponding each absorption tower is beaten slurries to spraying layer 3 from circulatory pool, being atomized into drop under the spraying layer nozzle act flows toward the bottom, absorption tower, with flue gas adverse current contact desulfuriation, the slurries after the desulfurization are collected by pipeline 14 through the conical hopper 16 of desulfurizing tower bottom and are introduced public oxidation pond 6 in the flow process.
Flue gas desulfur device sweetening process of the present invention is as follows:
The fume side process: the pending former flue gas of boiler enters the absorption tower from absorption tower body bottom inlet flue, by the recycle slurry liquid pump calcium-based slurries being evacuated to spraying layer from circulatory pool simultaneously atomizes, calcium-based slurries drop after the atomizing flows downward and contact with the pending flue gas adverse current that upwards flows and carries out desulfurization, and the flue gas after the desulfurization continues upwards to flow after the demister demist from the clean exhanst gas outlet outflow of desulfurizing tower bodies top;
Slurries side process:
Slurries side oxidation pond internal procedure: collect by the conical hopper of body bottom, absorption tower after absorption tower spray atomization slurry and the flue gas contact desulfuriation, and be incorporated into below the oxidation pond liquid level with pipe; In the oxidation pond the HSO that accepts in the desulfurization slurry to be contained
3 -Be blown into the oxidation air institute oxidation in the slurries; Oxidation pond is provided with the jacking-type agitator, plays the effect of stirring slurries on the one hand, plays on the other hand oxidation air fragmentation and peptizaiton; Take out the part slurries simultaneously in the oxidation pond and efflux and enter conventional gypsum dehydration system and carry out liquid-solid separation, the solid formation after the separation effluxes as desulfurizing byproduct, and the liquid phase thing after the separation returns oxidation pond.Oxidation pond is interior because HSO
3 -Under the formed H+ effect of oxidation, the pH value of slurries remains between the 4.0-5.0 naturally in oxidation pond, moves under low pH, helps the oxidation of calcium sulfite, the crystallization of gypsum and the dissolving of lime stone; Move under low pH, make calcium sulfite oxidation efficient height, desulfurizing byproduct Central Asia calcium sulphate content is few, makes the lime stone enhanced dissolution rate, and limestone content is few in the desulfurizing byproduct, and the desulfurizing byproduct quality improves; Under low pH, move, slurries are under sour environment, and the suction-operated of gypsum crystal face strengthens, and the directed velocity that forms crystal grain becomes big, help forming thick column (corynebacterium), compact structure, particle diameter distributes rationally, compression strength is high gypsum crystal grain, and be beneficial to the dehydration of gypsum filter cake.
Slurries side circulatory pool internal procedure: contained calcium sulfite passes through the central dividing plate overflow to circulating slot through the slurries of fully oxidation in the desulfurization slurry of accepting in the oxidation pond; In circulating slot, replenish lime stone slurry,, make the interior slurry pH value of circulating slot rise between the 6.0-6.5 by the dissolving of lime stone slurry; Slurries are beaten to spraying layer by circulating pump again in the circulatory pool.The jacking-type agitator is set on circulatory pool, play the effect of stirring slurries, make the solid particle in the slurries be in suspended state, also help the dissolving of lime stone, be beneficial to the rising of pH value in the circulatory pool, make not contain large quantities of lime stone in the loop slurry, be beneficial to the formation of low ph environment in the oxidation pond.
Slurries side desulfurizing tower internal procedure: circulating pump is beaten slurries to spraying layer from circulatory pool, being atomized into drop under the spraying layer nozzle act flows toward the bottom, absorption tower, with flue gas adverse current contact desulfuriation, the slurries after the desulfurization are collected by pipeline through the conical hopper of desulfurizing tower bottom and are introduced oxidation pond in the flow process.Slurries are the slurries of high pH value in the circulatory pool in the spray process, help SO in the flue gas
2Remove, and with respect to patent described in the background technology, the slurries of all spraying layers all are slurries of high pH value, more help the raising of desulfuration efficiency, are beneficial to reduce investment and operating cost; And the spray loop slurry is the fully gypsum slurries that contains small amount of limestone of oxidation of calcium sulfite, and the high pH value loop slurry that has solved patent described in the background technology is with unoxidized CaSO
3Be the slurries of main body, be easy to generate the fouling blocking problem under the consequent autoxidation effect.
Carry out following elaboration at device of the present invention:
The innovative point of wet desulphurization device of the present invention is to propose the corrective measure of cyclic oxidation groove, absorption tower bottom cycle oxidation trough is divided into two parts, a part is accepted the desulfurization slurry of outflow in the desulfurizing tower, carry out oxidation at this sulfite ion, from then on the desulfuration byproduct gypsum draws, and is called oxidation trough; And another part adds fresh lime stone slurry, and from then on slurries are introduced to spray in the absorption tower and carried out desulfurization, are called circulating slot.By this measure, make desulphurization system under two pH value environment, move.During design, according to coal-fired sulfur content, loop slurry time of staying in oxidation pond remains between the 2.5-5min, loop slurry in circulatory pool the time of staying generally between 1-2min.
The innovative point of wet desulphurization device of the present invention is to be collected by the conical hopper of body bottom, absorption tower after absorption tower spray atomization slurry and flue gas contact desulfuriation, and be incorporated into below the oxidation pond liquid level with pipe, oxidation pond agitator top, this design makes that on the one hand the flue gas that enters the absorption tower has the effect of water seal, on the other hand, enter from the absorption tower slurries of agitator can be rapidly effect by agitator be distributed to oxidation pond, be beneficial to the carrying out of physical-chemical reaction process in the groove, and after having avoided entering oxidation pond from the slurries that the absorption tower flows into the direct overflow of short circuit to circulatory pool.
The innovative point of wet desulphurization device of the present invention is that absorption tower bottom oxidation pond and circulatory pool adopt the cuboid design, and each pond top design jacking-type agitator has reduced the trouble point that conventional absorption tower side-feeding mixer is prone to fault.
The innovative point of wet desulphurization device of the present invention is between circulatory pool and oxidation pond dividing plate to be set, and contained calcium sulfite passes through the central dividing plate overflow to circulating slot through the slurries of fully oxidation in the desulfurization slurry of accepting in the oxidation pond.
The innovative point of wet desulphurization device of the present invention is with the cyclic oxidation groove of absorption tower bottom separately, can solve the contradictory problems of desulfurization degree and gypsum quality on certain degree.The pH value of slurries is far below pH value in the circulating slot in the oxidation trough, makes can keep than higher gypsum quality in the oxidation trough; Simultaneously, high circulating slot slurry pH value makes that slurry pH value improves in the absorption tower, and system's desulfurization degree is higher.When system can satisfy the desulfurization requirement, can suitably reduce the pH value in the charging spout, improve the quality of gypsum.When the boiler load increasing, or the sulfur content in fuel increase, in the time of can not satisfying the desulfurization requirement, can suitably improve the pH value in the charging spout, improve desulfurization degree, consider that from gypsum quality aspect the interior slurry pH value of charging spout should be lower than 6.5.
Claims (6)
1. dual grooved wet flue gas desulfurizer based on the operation of two pH values, described desulfurizer comprises absorption tower body (15), demister (2), spraying layer (3) and circulating pump (13), demister (2), spraying layer (3) from top to bottom are arranged in the top of absorption tower body (15), the lower end sidewall of absorption tower body (15) is provided with former smoke inlet (4), and the upper end sidewall of absorption tower body (15) is provided with clean exhanst gas outlet (1); It is characterized in that: described desulfurizer also comprises oxidation trough (6), circulating slot (10) and loop slurry return pipe (14), oxidation trough (6) and circulating slot (10) are arranged on the below of absorption tower body (15), and the upper end of the upper end of oxidation trough (6) and circulating slot (10) is communicated with; Absorption tower body (15) is communicated with oxidation trough (6) by loop slurry return pipe (14); Oxidation trough (6) is provided with gypsum slurries outlet (7), and oxidation trough (6) is provided with oxidation air inlet (8); Circulating slot (10) is provided with lime stone slurry inlet (9); Circulating pump (13) is used for that the loop slurry in the circulating slot (10) is evacuated to spraying layer (3) and locates into atomizing.
2. the dual grooved wet flue gas desulfurizer based on two pH value operations according to claim 1, it is characterized in that: described oxidation trough (6), circulating slot (10) are by cuboid pond body (17) and are arranged on interior dividing plate (11) formation of cuboid pond body (17), dividing plate (11) is divided into two parts as oxidation trough (6) and circulating slot (10) with the inner chamber of cuboid pond body (17) along its length direction, and the height of dividing plate (11) is lower than the height of cuboid pond body (17), and oxidation trough (6) and circulating slot (10) are connected.
3. the dual grooved wet flue gas desulfurizer based on two pH value operations according to claim 1, it is characterized in that: described desulfurizer also comprises two jacking-type agitators (5), in described oxidation trough (6) and the circulating slot (10) a jacking-type agitator (5) is set respectively; Loop slurry return pipe (14) liquid outlet is arranged at oxidation pond (6) below the liquid level, the top of jacking-type agitator (5).
4. according to claim 1,2 or 3 described dual grooved wet flue gas desulfurizers based on two pH value operations, it is characterized in that: described desulfurizer also comprises conical hopper (16), and described conical hopper (16) is arranged in the bottom of absorption tower body (15) and conical hopper (16) liquid outlet is connected with loop slurry return pipe (14).
5. method of utilizing claim 1,2,3 or 4 described desulfurizers to carry out wet process of FGD, it is characterized in that: described method sweetening process is as follows:
Step 1, the pending former flue gas of boiler enter in the absorption tower body (15) from absorption tower body (15) the former smoke inlet in bottom (4), by circulating pump (13) calcium-based slurries being evacuated to spraying layer (3) from circulating slot (10) simultaneously atomizes, calcium-based slurries drop after the atomizing flows downward and contact with the pending flue gas adverse current that upwards flows and carries out desulfurization, and the flue gas after the desulfurization continues upwards to flow after demister (2) demist from clean exhanst gas outlet (1) outflow of desulfurizing tower bodies top;
Collect by the conical hopper (16) of body bottom, absorption tower after step 2, absorption tower body (15) spray atomization slurry and the flue gas contact desulfuriation, and be incorporated into oxidation trough (6) below the liquid level with loop slurry return pipe (14); In the oxidation trough (6) the HSO that accepts in the desulfurization slurry to be contained
3 -Be blown into the oxidation air institute oxidation in the slurries by oxidation air inlet (8); By jacking-type agitator (5) slurries in the oxidation trough (6) are stirred; Taking out the part slurries simultaneously in the oxidation trough (6) effluxes and enters conventional gypsum dehydration system and carry out liquid-solid separation, solid formation after the separation effluxes as desulfurizing byproduct, liquid phase thing after the separation returns in the oxidation trough (6), and the pH value of the interior slurries of oxidation trough (6) remains between the 4.0-5.5;
Contained calcium sulfite passes through central dividing plate (11) overflow to circulating slot (10) through the slurries of fully oxidation in the desulfurization slurry of accepting in step 3, the oxidation trough (6); In circulating slot (10), replenish lime stone slurry,, make the interior slurry pH value of circulating slot (10) rise between the 6.0-6.5 by the dissolving of lime stone slurry; And the slurries in the circulating slot (10) are stirred by jacking-type agitator (5);
Step 4, the interior slurries of circulating slot (10) are beaten to spraying layer by circulating pump (13) and are carried out desulfurization, being atomized into drop under the spraying layer nozzle act flows to the bottom, absorption tower, with flue gas adverse current contact desulfuriation, the slurries after the desulfurization are collected by loop slurry return pipe (14) through the conical hopper (16) of desulfurizing tower bottom and are introduced in the oxidation trough (6) in the flow process.
6. the method for wet process of FGD according to claim 5, it is characterized in that: loop slurry time of staying in oxidation pond remains on 2.5-5min, and loop slurry time of staying in circulatory pool remains at 1-2min.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010608773 CN102091519A (en) | 2010-12-28 | 2010-12-28 | Double-groove wet-process flue gas desulfuration device and method operating on basis of two pH values |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010608773 CN102091519A (en) | 2010-12-28 | 2010-12-28 | Double-groove wet-process flue gas desulfuration device and method operating on basis of two pH values |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102091519A true CN102091519A (en) | 2011-06-15 |
Family
ID=44124895
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201010608773 Pending CN102091519A (en) | 2010-12-28 | 2010-12-28 | Double-groove wet-process flue gas desulfuration device and method operating on basis of two pH values |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102091519A (en) |
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102600701A (en) * | 2012-01-13 | 2012-07-25 | 浙江天蓝环保技术股份有限公司 | Wet flue gas desulfurization process and device |
| CN102949923A (en) * | 2011-08-30 | 2013-03-06 | 威海鑫山集团有限公司 | Method and device for removing sulfur dioxide in industrially-sintered flue gas and recovering gypsum |
| CN102974201A (en) * | 2011-08-08 | 2013-03-20 | 同方环境股份有限公司 | Double pH adjustment flue gas desulphurization system and control method thereof |
| CN103566744A (en) * | 2013-11-21 | 2014-02-12 | 航天环境工程有限公司 | Gas liquid mixing wet type exhaust smoke desulfurization device for sintering machine |
| CN105536494A (en) * | 2015-12-30 | 2016-05-04 | 廖厚伍 | Single-tower pH double-region double-circulation desulfurization process |
| CN108310950A (en) * | 2018-04-10 | 2018-07-24 | 李威 | The device of processing is absorbed for industrial waste gas |
| CN109028122A (en) * | 2018-07-02 | 2018-12-18 | 广德县坚固水泥制品有限公司 | Numb stone wet dedusting formula energy-saving coal fired boiler |
| CN109045906A (en) * | 2018-08-28 | 2018-12-21 | 山东神华山大能源环境有限公司 | A kind of Integral tower, devices and methods therefor for realizing the gas cleaning containing coal dust |
| CN109381989A (en) * | 2018-11-05 | 2019-02-26 | 华电电力科学研究院有限公司 | The system and its working method of Multi-stage cooling cooperation-removal multiple pollutant in a kind of tower |
| CN109499304A (en) * | 2018-12-27 | 2019-03-22 | 朱敬 | The device and technique of sulfur dioxide in a kind of efficient removal coal-fired flue-gas |
| CN110026076A (en) * | 2019-05-14 | 2019-07-19 | 内蒙古霍煤创源矿业有限公司 | A kind of electrolytic aluminum smoke device for deep cleaning and method |
| CN111617604A (en) * | 2020-06-05 | 2020-09-04 | 碧水蓝天环境工程有限公司 | Energy-saving and environment-friendly limestone-gypsum wet flue gas desulfurization tower |
| CN111905536A (en) * | 2020-06-17 | 2020-11-10 | 天津国电津能滨海热电有限公司 | Automatic control system for pH value of slurry passing through desulfurization absorption tower |
| CN117398821A (en) * | 2023-10-19 | 2024-01-16 | 江苏龙泰环保设备制造有限公司 | Wet electric purification system for sulfur-containing tail gas desulfurization after incineration |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201058277Y (en) * | 2007-06-21 | 2008-05-14 | 山东大学 | Wet desulfurizing device with cross flow double circles in air flow |
| CN101874976A (en) * | 2009-12-18 | 2010-11-03 | 哈尔滨工业大学 | Desulfuration method by supplementing air to enhance low-load adaptability based on wet desulfuration tower |
-
2010
- 2010-12-28 CN CN 201010608773 patent/CN102091519A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201058277Y (en) * | 2007-06-21 | 2008-05-14 | 山东大学 | Wet desulfurizing device with cross flow double circles in air flow |
| CN101874976A (en) * | 2009-12-18 | 2010-11-03 | 哈尔滨工业大学 | Desulfuration method by supplementing air to enhance low-load adaptability based on wet desulfuration tower |
Cited By (21)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102974201A (en) * | 2011-08-08 | 2013-03-20 | 同方环境股份有限公司 | Double pH adjustment flue gas desulphurization system and control method thereof |
| CN102974201B (en) * | 2011-08-08 | 2014-07-02 | 同方环境股份有限公司 | Double pH adjustment flue gas desulphurization system and control method thereof |
| CN102949923A (en) * | 2011-08-30 | 2013-03-06 | 威海鑫山集团有限公司 | Method and device for removing sulfur dioxide in industrially-sintered flue gas and recovering gypsum |
| CN102600701A (en) * | 2012-01-13 | 2012-07-25 | 浙江天蓝环保技术股份有限公司 | Wet flue gas desulfurization process and device |
| CN103566744A (en) * | 2013-11-21 | 2014-02-12 | 航天环境工程有限公司 | Gas liquid mixing wet type exhaust smoke desulfurization device for sintering machine |
| CN103566744B (en) * | 2013-11-21 | 2015-11-04 | 航天环境工程有限公司 | Sintering machine gas-liquid mixed wet type flue gas desulfurization equipment |
| CN105536494A (en) * | 2015-12-30 | 2016-05-04 | 廖厚伍 | Single-tower pH double-region double-circulation desulfurization process |
| CN108310950B (en) * | 2018-04-10 | 2019-02-01 | 李威 | The device of processing is absorbed for industrial waste gas |
| CN108310950A (en) * | 2018-04-10 | 2018-07-24 | 李威 | The device of processing is absorbed for industrial waste gas |
| CN109028122A (en) * | 2018-07-02 | 2018-12-18 | 广德县坚固水泥制品有限公司 | Numb stone wet dedusting formula energy-saving coal fired boiler |
| CN109045906A (en) * | 2018-08-28 | 2018-12-21 | 山东神华山大能源环境有限公司 | A kind of Integral tower, devices and methods therefor for realizing the gas cleaning containing coal dust |
| CN109045906B (en) * | 2018-08-28 | 2024-05-24 | 国能(山东)能源环境有限公司 | Integrated tower, device and method for realizing purification of flue gas containing coal dust |
| CN109381989A (en) * | 2018-11-05 | 2019-02-26 | 华电电力科学研究院有限公司 | The system and its working method of Multi-stage cooling cooperation-removal multiple pollutant in a kind of tower |
| CN109499304A (en) * | 2018-12-27 | 2019-03-22 | 朱敬 | The device and technique of sulfur dioxide in a kind of efficient removal coal-fired flue-gas |
| CN110026076B (en) * | 2019-05-14 | 2024-04-16 | 内蒙古创源金属有限公司 | Electrolytic aluminum flue gas deep purification device and method |
| CN110026076A (en) * | 2019-05-14 | 2019-07-19 | 内蒙古霍煤创源矿业有限公司 | A kind of electrolytic aluminum smoke device for deep cleaning and method |
| CN111617604A (en) * | 2020-06-05 | 2020-09-04 | 碧水蓝天环境工程有限公司 | Energy-saving and environment-friendly limestone-gypsum wet flue gas desulfurization tower |
| CN111905536B (en) * | 2020-06-17 | 2022-05-24 | 天津国能津能滨海热电有限公司 | Automatic control system for pH value of slurry passing through desulfurization absorption tower |
| CN111905536A (en) * | 2020-06-17 | 2020-11-10 | 天津国电津能滨海热电有限公司 | Automatic control system for pH value of slurry passing through desulfurization absorption tower |
| CN117398821A (en) * | 2023-10-19 | 2024-01-16 | 江苏龙泰环保设备制造有限公司 | Wet electric purification system for sulfur-containing tail gas desulfurization after incineration |
| CN117398821B (en) * | 2023-10-19 | 2024-04-05 | 江苏龙泰环保设备制造有限公司 | Wet electric purification system for sulfur-containing tail gas desulfurization after incineration |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102091519A (en) | Double-groove wet-process flue gas desulfuration device and method operating on basis of two pH values | |
| JP6223654B2 (en) | Flue gas desulfurization equipment | |
| CN102755827B (en) | Flue gas desulfurization process and device adopting acetylene sludge-gypsum method | |
| CN105817134A (en) | Chemical process wet-method desulphurization technology | |
| US20120189522A1 (en) | Method of Desulfurizing Flue Gas, an Arrangement for Desulfurizing Flue Gas, and a Method of Modernizing a Desulfurization Arrangement | |
| CN102764580B (en) | A kind of apparatus and method of white clay/carbide slag-gypsum wet flue gas desulfurizing | |
| CN103349902B (en) | Flue gas processing method | |
| CN1309456C (en) | Hopper type current-collecting device of flue-gas desulphurization system by shunting method or external inforced oxidizing process | |
| CN101703861B (en) | Process and device for desulphurizing flue gas by lime-gypsum method | |
| CN104959012A (en) | Magnesium-calcium based wet method desulphurization system and method for removing sulfur dioxide in flue gas and producing gypsum | |
| CN101844036A (en) | Wet flue gas desulfurization (WFGD) process for gypsum through oxidization in tower by using calcium-based strongly basic substance | |
| CN102284238A (en) | Bialkali-method flue-gas desulphurization process | |
| CN106139877A (en) | Efficient small coal-firing units gas desulfurization device | |
| CN116440692A (en) | Wet desulfurization system and method for flue gas carbide slag of coal-fired power plant | |
| CN203090752U (en) | Double-pool wet-process flue gas dedusting and desulfurizing equipment | |
| CN204543981U (en) | Removing sulfur dioxide in flue gas also produces the magnesium-calcium base wet-process desulphurization system of gypsum | |
| CN101306319A (en) | Direct discharging flue gas treatment method | |
| CN104226102B (en) | A kind of aluminium electrolytic flue horizontal spraying desulfurizer and method | |
| CN101791513A (en) | Jacking-type exhaust-gas treatment device and method | |
| CN201578988U (en) | Double circulation double alkali method flue gas desulfurization device | |
| CN201371033Y (en) | Novel mixed flow type flue gas washing tower | |
| CN203507812U (en) | Single-tower double-medium desulfurizer | |
| CN202751947U (en) | Flue gas desulfurization (FGD) device using carbide slag-gypsum method | |
| CN201260936Y (en) | Wet flue gas desulfurization absorption tower slurry pool | |
| JP4933121B2 (en) | Combustion exhaust gas purifier with separated cleaning liquid reservoir |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20110615 |