CN1962035A - Spray cyclone bed type gas liquid solid tri-phase reactor - Google Patents
Spray cyclone bed type gas liquid solid tri-phase reactor Download PDFInfo
- Publication number
- CN1962035A CN1962035A CN 200610104818 CN200610104818A CN1962035A CN 1962035 A CN1962035 A CN 1962035A CN 200610104818 CN200610104818 CN 200610104818 CN 200610104818 A CN200610104818 A CN 200610104818A CN 1962035 A CN1962035 A CN 1962035A
- Authority
- CN
- China
- Prior art keywords
- slurry
- gas
- liquid
- phase
- slurry pool
- 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
- 239000007787 solid Substances 0.000 title claims abstract description 11
- 239000007788 liquid Substances 0.000 title abstract description 16
- 239000007921 spray Substances 0.000 title description 6
- 239000002002 slurry Substances 0.000 claims abstract description 79
- 238000007254 oxidation reaction Methods 0.000 claims description 19
- 230000003647 oxidation Effects 0.000 claims description 13
- 239000012071 phase Substances 0.000 abstract description 11
- 239000007790 solid phase Substances 0.000 abstract description 10
- 238000006243 chemical reaction Methods 0.000 abstract description 9
- 239000002245 particle Substances 0.000 abstract description 8
- 238000002156 mixing Methods 0.000 abstract description 5
- 239000007791 liquid phase Substances 0.000 abstract description 4
- 230000001590 oxidative effect Effects 0.000 abstract description 3
- 238000003756 stirring Methods 0.000 abstract description 3
- 238000000034 method Methods 0.000 abstract description 2
- 230000000694 effects Effects 0.000 abstract 1
- 238000005507 spraying Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 14
- 238000010521 absorption reaction Methods 0.000 description 13
- 238000006477 desulfuration reaction Methods 0.000 description 5
- 230000023556 desulfurization Effects 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- 235000019738 Limestone Nutrition 0.000 description 4
- 239000006028 limestone Substances 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 238000013019 agitation Methods 0.000 description 3
- 239000010440 gypsum Substances 0.000 description 3
- 229910052602 gypsum Inorganic materials 0.000 description 3
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 230000003009 desulfurizing effect Effects 0.000 description 2
- 238000010304 firing Methods 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000011505 plaster Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000001143 conditioned effect Effects 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000013016 damping Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000010667 large scale reaction Methods 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000012857 repacking Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000008247 solid mixture Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Images
Landscapes
- Treating Waste Gases (AREA)
Abstract
喷射旋流床式气液固三相反应器，使用若干台循环泵，将浆料池内的浆液从四角或四墙部位抽出，经循环泵的加速后形成多股高速射流从浆料池的周围切向喷入浆料池，驱动浆料池整体旋转，替代了机械桨叶搅拌器对浆料池的搅拌作用。整个流场大致上形成稳定的单一旋转流场，可以较为方便地控制固相颗粒的分选过程。而氧化空气直接在高速射流的喷口内投入，液相和气相有很大的速度差，高速的液相将气泡击碎，大大强化了气液之间的混合，可提高气液反应强度，另外，气相在浆池中形成螺旋运动的轨迹而不是自由上浮的状态，会延长气泡在浆池中的停留时间，从而提高氧化空气的利用率。
The jet swirl bed type gas-liquid-solid three-phase reactor uses several circulating pumps to extract the slurry in the slurry pool from the four corners or four walls, and after being accelerated by the circulating pump, multiple high-speed jets flow from the surrounding of the slurry pool. Tangential spraying into the slurry tank drives the overall rotation of the slurry tank, replacing the stirring effect of the mechanical paddle agitator on the slurry tank. The entire flow field roughly forms a stable single rotating flow field, which can control the sorting process of solid phase particles more conveniently. The oxidizing air is directly injected into the nozzle of the high-speed jet, and there is a large speed difference between the liquid phase and the gas phase. The high-speed liquid phase crushes the bubbles, which greatly strengthens the mixing between the gas and liquid, and can increase the gas-liquid reaction intensity. , The gas phase forms a spiral trajectory in the pulp tank instead of a free floating state, which will prolong the residence time of the bubbles in the pulp tank, thereby improving the utilization rate of oxidizing air.
Description
Technical field
The invention belongs to the phase reactor technical field, be specifically related to a kind of spray cyclone bed type gas liquid solid tri-phase reactor that is used for the slurries pond of large-scale wet process of FGD.
Background technology
SO is finished in wet desulphurization in the absorption tower
2Absorption, and in the slurries pond, finish SO
2Oxidation and curing.The slurries pond is the vitals that gas-solid mixture absorbs gas, bearing separating of gas and absorption liquid, the neutralization of absorption liquid, vital tasks such as gypsum oxidation and crystallization, its ruuning situation have directly determined the mass concentration of absorption liquid, the situation that chemical reaction carries out and the quality of discharging material.
The main function in slurries pond is: the modulation slurries: the fresh water of fresh agstone (or limestone slurry) and supply needs at first fully to mix in stock tank, and allotment becomes the desulfurization slurry of suitable concn and composition; Oxidation CaSO
3: oxidation air is directly imported the slurries pond, with the slurries that fall after rise in the absorption tower (because of with SO
2Reaction generates a large amount of CaSO
3) carry out oxidation reaction, with CaSO
3Be oxidized to CaSO
4, can this link not only is related to realize fully that solid sulphur is (the CaSO of easy decomposition
3Be converted into stable CaSO
4), also be directly connected to the situation of slurries pipeline scale; Regulate slurry pH value and other composition: the input situation of the equilibrium condition of various materials and additive will determine pH value and other composition of the slurries that circulate in the slurries pond in system, and the pH value of slurries is directly connected in the absorption tower SO
2Absorbability, also influence CaSO
3The carrying out of oxidation reaction, the adjusting of pH value need be carried out in the slurries pond; Liquid-solid separation: because gypsum must crystallization and grows to certain particle diameter, could be as qualified byproduct discharge, other impurity (mainly is CaCO in the calcium plaster that also will guarantee simultaneously to discharge
3And CaSO
3) content be within the restricted portion, at this moment, must rationalization liquid-solid separation process in the slurries pond, guarantee the sorting quality of gypsum particle; The conditioned reaction thing time of staying: in the design of the slurries pond of wet desulphurization, there are three important time of staying to be guaranteed, the one, as the time of staying of limestone particle in system of desulfurizing agent, because lime stone is a kind of indissoluble material, under solutions of weak acidity, approximately need 8～14 hours molten finishing that just can disappear, in system, have the sufficient time of staying could guarantee that lime stone fully participates in desulphurization reaction so must guarantee it; The 2nd, enter the time of staying of the loop slurry on absorption tower, because the slurries that fall after rise are to absorbing SO from the absorption tower
2Be a kind of near saturated state, must in the slurries pond, stop time enough, make SO
3 2-Fully be converted into other composition (as the CaCO of solid phase
3, CaSO
4Or SO
4 2-), could possess absorption SO again
2Ability and enter the absorption tower once more; The 3rd, as the time of staying of oxidation air in system of oxidant, oxygen is not a kind of gas soluble in water, could participate in CaSO and oxygen must be dissolved in slurries
3Oxidation reaction, so must guarantee that oxidation air has enough time of staying in stock tank, could guarantee oxidation reaction carry out the degree of depth and oxidation air has higher utilization rate.More than three kinds of time of staying coupling mutually also, to guarantee fully finishing of various desulfurization, desulfurization reaction; System buffer: each parameter of desulphurization system is constantly to change at run duration, load variations such as station boiler causes exhaust gas volumn to change, the ature of coal variation of burning causes smoke components to change, the composition of agstone changes and the variation of the various parameters that other possible situation of whole system causes, and under the situation that these parameters change, whole system should be stable rather than responsive, guarantee the desulfurization degree of flue gas, discharge the quality of calcium plaster and the stable operation of system itself, at this moment, the pH value of slurries, the slurries main component, obvious variation should not take place in the particle diameter of solid phase particles and distribution situation etc., just need guarantee by the physical buffer and the chemical buffer capacity in slurries pond self.
In the wet desulfurization system, the slurries pond also is the higher parts of fault rate, in the strength of materials, overflowing with all many-sides such as engineering efficient of damping, slurries is installed remains in problem.Traditional slurries pond is to adopt churned mechanically bubbling bed reactor, oxidation air is imported from bottom, slurries pond or agitator the place ahead by the air input pipe, adopts the general stock tank of vertical agitator only to arrange an agitator, and flow field structure is simple relatively, the solid phase sorting is good, still.For the boiler unit more than the 300MW, the diameter of propeller blade of agitator is more than 10 meters and even 15 meters, itself structure heaviness not only, and arrange for the absorption tower of slurries pond top and to bring certain difficulty, must adopt the arranged off-centre mode of absorption tower and slurries pond decentraction this moment, perhaps must adopt Double-Tower Structure; Adopt sidewall mechanical agitation mode, the number of agitator can increase, but the situation of whole slurries pond flow field is very complicated, be difficult to take into account the problem of solid phase sorting, and the force-bearing situation of stock tank wall is not good, be sealed with certain difficulty, the situation generation that has slurries to leak often between rotating shaft simultaneously and the stock tank wall.
The main shortcoming of this reactor is: owing to will look after the sorting of solid phase, churned mechanically flow velocity can not very high about 50r/min, the bubble of oxidation air is a kind of state that freely floats basically, gas-liquid mixed is strong inadequately, oxidation reaction speed is relatively slow, and in a single day break down, the utilization rate of oxidation air is lower than 30%; Desulfurizing tower belongs to large-scale reaction unit, and mechanical agitator is when maximizing, and the structure heaviness, is difficult to layouts, fault rate height, inconvenient maintenance and necessary shutdown maintenance.
Summary of the invention
The objective of the invention is to overcome the shortcoming of above-mentioned prior art, a kind of mechanical agitation parts that need not are provided, can prevent the spray cyclone bed type gas liquid solid tri-phase reactor of fouling, wearing and tearing and other mechanical part fault.
For achieving the above object, the technical solution used in the present invention is: comprise slurry pool, on the wall of slurry pool, respectively be furnished with one or more slurry circulating pump, the inlet of this slurry circulating pump and outlet be the outlet by pipeline and slurries pond and send into mouth and be connected respectively, the pipeline of sending into mouthful also is connected with the oxidation air pipeline, and outlet and send into mouthful to cut angle with four jiaos of slurry pool or four walls be 5 °～40 °.
Because the present invention uses some circulating pumps, slurries in the slurry pool are extracted out from four jiaos or four wall positions, after the acceleration of circulating pump, form the multiply high-speed jet and around slurry pool, tangentially spray into slurry pool, drive the whole rotation of slurry pool, substituted the stirring action of mechanical blade agitator slurry pool.Whole flow field forms stable single rotational flow field haply, can control the assorting room of solid phase particles comparatively easily.And oxidation air directly drops in the spout of high-speed jet, liquid and gas have very big speed difference, liquid phase at a high speed smashes bubble, strengthened the mixing between the gas-liquid greatly, can improve gas liquid reaction intensity, in addition, gas phase forms the track of screw rather than the state that freely floats in stock tank, the time of staying of bubble in stock tank can be prolonged, thereby improve the utilization rate of oxidation air, and the present invention only need use some circulating pumps and connecting pipe, arrangement convenience is flexible, save heavy mechanical agitation blade, very helped the maximization of reactor.
Description of drawings
Fig. 1 is an overall structure schematic diagram of the present invention.
The specific embodiment
Below in conjunction with accompanying drawing the present invention is described in further detail.
Referring to Fig. 1, the present invention includes slurry pool 1, on the wall of slurry pool 1, respectively be furnished with a slurry circulating pump 2, system's when operation slurries are drawn to be delivered to by slurry circulating pump 2 by outlet 3 and are sent into mouthfuls 4 and reenter slurry pool 1, the outlet 3 of slurry pool 1 is 5 °～40 ° with sending into mouth 4 with four jiaos of slurry pool 1 or the corner cut of four walls, can form the two-layer of current in slurry pool 1 after being provided with according to this angle horizontally rotates, thereby the turbulence that realizes the solution-air two-phase mixes, this situation is similar to the corner tangential firing in the suspension firing stove, thereby reaches the Expected Results of stirring.
When if the diameter of slurry pool is bigger, the present invention is furnished with many slurry circulating pumps 2 on four jiaos of slurry pool 1 or wall, and these many slurry circulating pumps 2 are on same horizontal plane.
If slurry pool 1 is when higher, the present invention is furnished with many slurry circulating pump 2 on the short transverse of the wall upper edge of slurry pool 1 slurry pool 1.
The present invention has multiply high-speed gas-liquid mixing jet tangentially to spray into slurry pool 1 around slurry pool 1, and the momentum of these jets is enough to drive slurry pool 1 whole rotation, and the gas-liquid two-phase mixing is strong, also satisfies the needs of slurry pool 1 mass transfer; Gas-liquid-solid three phase flow in the slurry pool 1 is eddy flow on the whole, can keep stronger liquid-solid mixing intensity, and form rational solid phase layering, realizes the reasonable sorting to solid phase particles; There is not mechanical agitator, but can be by regulating effluxvelocity, the concentration of dynamic adjustments solid phase and size distribution make it to reach the requirement of grain sorting.The gas of participation reaction is promptly sent in the mouth 4 from efflux nozzle and is fed, and gas-liquid phase velocity difference is big, and gas is forced to pulverize and is minute bubbles, and specific area is big, the time of staying is long, and gas liquid reaction is strong.Also can be as required in slurry pool 1 bottom or send into outside mouthfuls 4 and feed gas, be easy to realize repacking to existing equipment.
Claims (1)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200610104818 CN1962035A (en) | 2006-10-30 | 2006-10-30 | Spray cyclone bed type gas liquid solid tri-phase reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200610104818 CN1962035A (en) | 2006-10-30 | 2006-10-30 | Spray cyclone bed type gas liquid solid tri-phase reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1962035A true CN1962035A (en) | 2007-05-16 |
Family
ID=38081364
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200610104818 Pending CN1962035A (en) | 2006-10-30 | 2006-10-30 | Spray cyclone bed type gas liquid solid tri-phase reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1962035A (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102019158A (en) * | 2010-11-01 | 2011-04-20 | 沈阳化工大学 | Tubular gas-liquid reactor capable of realizing synchronization of rotational flow and injection |
| CN103316576A (en) * | 2013-05-14 | 2013-09-25 | 宜兴市化工成套设备有限公司 | Desulfurizing and demisting combined tower |
| WO2015195051A1 (en) * | 2014-06-20 | 2015-12-23 | National University Of Singapore | Triphasic flow millireactors |
| CN106732259A (en) * | 2016-12-13 | 2017-05-31 | 衡阳华砷科技有限公司 | A kind of stirring means of reaction vessel |
| CN107020007A (en) * | 2017-06-05 | 2017-08-08 | 成都绿水科技有限公司 | A kind of economic benefits and social benefits reaction of high order type desulfurization slurry oxidization processing system and technique |
| CN108130265A (en) * | 2017-07-07 | 2018-06-08 | 北京昊海天际科技有限公司 | A kind of method for stirring fermentation materials in dry fermentation tank |
| CN112827344A (en) * | 2021-02-07 | 2021-05-25 | 华南理工大学 | A kind of jet extraction desulfurization tower slurry oxidation device and method |
-
2006
- 2006-10-30 CN CN 200610104818 patent/CN1962035A/en active Pending
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102019158A (en) * | 2010-11-01 | 2011-04-20 | 沈阳化工大学 | Tubular gas-liquid reactor capable of realizing synchronization of rotational flow and injection |
| CN102019158B (en) * | 2010-11-01 | 2013-06-19 | 沈阳化工大学 | Tubular gas-liquid reactor capable of realizing synchronization of rotational flow and injection |
| CN103316576A (en) * | 2013-05-14 | 2013-09-25 | 宜兴市化工成套设备有限公司 | Desulfurizing and demisting combined tower |
| WO2015195051A1 (en) * | 2014-06-20 | 2015-12-23 | National University Of Singapore | Triphasic flow millireactors |
| US9850184B2 (en) | 2014-06-20 | 2017-12-26 | National University Of Singapore | Triphasic flow millireactors |
| CN106732259A (en) * | 2016-12-13 | 2017-05-31 | 衡阳华砷科技有限公司 | A kind of stirring means of reaction vessel |
| CN107020007A (en) * | 2017-06-05 | 2017-08-08 | 成都绿水科技有限公司 | A kind of economic benefits and social benefits reaction of high order type desulfurization slurry oxidization processing system and technique |
| CN108130265A (en) * | 2017-07-07 | 2018-06-08 | 北京昊海天际科技有限公司 | A kind of method for stirring fermentation materials in dry fermentation tank |
| CN112827344A (en) * | 2021-02-07 | 2021-05-25 | 华南理工大学 | A kind of jet extraction desulfurization tower slurry oxidation device and method |
| CN112827344B (en) * | 2021-02-07 | 2025-02-11 | 华南理工大学 | A slurry oxidation device and method for jet exhaust desulfurization tower |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1962035A (en) | Spray cyclone bed type gas liquid solid tri-phase reactor | |
| CN205462756U (en) | Counterattack formula annular space sprays stirring formula flotation device of breathing in | |
| CN205704706U (en) | A kind of mixer with Double stirring function | |
| US8323359B2 (en) | Multi-stage crystallization apparatus and method | |
| JPWO2007066443A1 (en) | Wet flue gas desulfurization apparatus and wet flue gas desulfurization method | |
| CN105148823A (en) | Inflatable stirring reaction device | |
| CN203855461U (en) | Double-impeller surface aerating device | |
| CN203469801U (en) | Desulfurized ash-limestone mixing and slurrying device | |
| CN102553426A (en) | Process and system for preparing wet desulphurization agent by utilizing desulfurization ash | |
| CN206051675U (en) | A kind of gas-liquid mixed solid stirring system under the conditions of anaerobic reaction | |
| CN205518239U (en) | Counterattack formula annular space sprays agitator of breathing in | |
| CN201260936Y (en) | Wet flue gas desulfurization absorption tower slurry pool | |
| CN105381887B (en) | A slurry mixing tank for fine mineral flotation | |
| CN208082270U (en) | A kind of Novel mixer | |
| CN216878718U (en) | Desulfurizer supply device for low-temperature flue gas desulfurization | |
| CN101940889B (en) | Method and device for mixing mechanical agitation with bubble agitation | |
| CN109205811A (en) | A kind of stirring aerating system and the application certainly of flue gas desulphurization system waste water regulating box | |
| CN201171965Y (en) | Pneumatic energy-saving stirring device of thionizer | |
| CN201505506U (en) | Flue gas desulfurization absorption tower | |
| CN205462757U (en) | Counterattack formula annular space from taking fairing sprays stirring formula flotation device of breathing in | |
| CN210009826U (en) | Limestone gypsum wet desulphurization device | |
| CN201436060U (en) | Gas outburst spinning dive absorption tower by wet process of flue gas desulphurization | |
| CN205413365U (en) | A stirred tank of sizing mixing that is used for flotation of fine grain mineral | |
| CN209428243U (en) | A kind of stirring aerating system certainly of flue gas desulphurization system waste water regulating box | |
| CN204897753U (en) | A digestion device for evaporating press standard brick |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C12 | Rejection of a patent application after its publication | ||
| RJ01 | Rejection of invention patent application after publication |
Open date: 20070516 |