CN100358623C - Homogeneous-phase fluidized bed reactor - Google Patents
Homogeneous-phase fluidized bed reactor Download PDFInfo
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- CN100358623C CN100358623C CNB2005100249617A CN200510024961A CN100358623C CN 100358623 C CN100358623 C CN 100358623C CN B2005100249617 A CNB2005100249617 A CN B2005100249617A CN 200510024961 A CN200510024961 A CN 200510024961A CN 100358623 C CN100358623 C CN 100358623C
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Abstract
The present invention relates to a homogeneous phase fluidized bed reactor, which comprises a reaction box, wherein the side wall of the reaction box is provided with a raw material liquid inlet, a reaction liquid inlet and a slag discharging opening. The present invention also comprises a steady flow settling box which is above the reaction box and a static state settling box which is above the steady flow settling box, the opening of the upper part of the reaction box is communicated with the steady flow settling box and the side wall is uniformly distributed with two or more than two stirrers. The steady flow settling box is a cavity, the upper and the lower parts of which are opened, the opening of the lower part is communicated with the reaction box, the opening of the upper part is communicated with the static state settling box and the steady flow settling box comprises a plurality of layers of retainer rings which are arranged alternately. The opening of the lower part of the static state settling box is communicated with the opening of the upper part of the steady flow settling box, the caliber of the opening of the lower part of the static state settling box is larger than the caliber of the opening of the upper part of the reaction box and the static state settling box is provided with a liquid cleaning opening. The generation of little calcium sulphate and the scale formation can be prevented by the homogeneous phase fluidized bed reactor, the required calcium ion molar concentration can be decreased to that Ca <2 +>: SO4 <2-> is larger than 1.5: 1, the cost and energy sources are reduced and the present invention is favorable for the popularization of the method of nitre removal with the calcium method.
Description
Technical field
The present invention relates to a kind of flow reactor, relate in particular to a kind of homogeneous-phase fluidized bed reactor that adopts the calcium method to remove sulfate radical in the production of caustic soda.
Background technology
Caustic soda is widely used in papermaking, daily washing, field of light industry as important industrial materials, especially occupies an important position in petroleum chemical industry (chemical and medicine industry, glass, enamel, process hides, food production) field.In China, a lot of producers adopt high awns bittern system caustic soda, raising along with caustic soda production, the particularly raising of barrier film high concentration liquid caustic soda and ionic membrane caustic soda output, the sulfate radical that produces in the production is cumulative in the whole production system, more and more be difficult to handle, restricting the normal operation of caustic soda equipment, ordinary production is caused adverse influence.For the processing of sulfate radical, China adopts the barium method to remove nitre, and minority producer adopts the calcium method to remove nitre.Comparatively speaking, remaining barium ions exceeds standard easily in the barium sulfate sedimentation separation difficulty that though that the barium method is removed the nitre effect is better, required expense is higher, produce, the secondary refined brine, because barium ions itself is poisonous, can producers' health be worked the mischief simultaneously; And the calcium method is removed nitre employing CaCl at present
2With SO
4 2-Reaction generates CaSO
4Precipitation (I) is more after filtration with CaSO
4Precipitation is filtering from salt solution, thereby removes sulfuric acid
CaCl
2+SO
4 2-+2H
2O＝CaSO
4·2H
2O↓+2Cl
- (I)
Root.Though removing nitre, the calcium method can reach the purpose of removing sulfate radical, because CaSO
4Belong to the slightly soluble material in water, solubility is bigger in salt solution, for example, under common reaction temperature, Ca
2+Concentration when being 1.7g/L, SO
4 2-Concentration be 2.36g/L; Reach the requirement of the concentration that makes sulfate ion, then need Ca less than 2g/L
2+Molar concentration reach Ca
2+: SO
4 2-＞2: 1, therefore must increase consumption with calcium ion, increased the consumption of calcium ion, increased the cost of the unnecessary calcium ion of post processing simultaneously; The calcium method is removed the CaSO that reaction generates in the nitre processing commonly used in addition
4Particle is tiny, and sedimentation coefficient SV30 is difficult to realize Separation of Solid and Liquid greater than 50%.These effects limit the calcium method remove the low-cost advantage of nitre, and influenced the calcium method and removed nitre promoting the use of in production of caustic soda enterprise.
Summary of the invention
One of purpose of the present invention provides and a kind ofly adopts the calcium method to remove the sulfate radical that accumulates in the production of caustic soda and prevent CaSO
4Generate tiny particle and fouling, make reaction reach balance, SO simultaneously at a certain temperature
4 2-Ion obtains under the maximum depositing technology condition, and the molar concentration rate of required calcium ion reduces to Ca
2+: SO
4 2-＞1.5: 1 homogeneous-phase fluidized bed reactor.
For achieving the above object, the invention provides a kind of homogeneous-phase fluidized bed reactor, comprise a reaction chamber, the sidewall of described reaction chamber is provided with material liquid import, reactant liquor import and slag-drip opening, it is characterized in that, described homogeneous-phase fluidized bed reactor comprises that also one is arranged on the current stabilization flow tank on the described reaction chamber, and a static flow tank that is arranged on the described current stabilization flow tank; The upper opening of described reaction chamber, and join with described current stabilization flow tank and to be communicated with, along also evenly being laid with two or more agitators in the sidewall of described reaction chamber; Described current stabilization flow tank is equal cavity of opening up and down, its underpart opening joins to be communicated with described reaction chamber with the upper opening of described reaction chamber, its upper opening joins with described static flow tank and is communicated with, and described current stabilization flow tank comprises the spaced back-up ring of multilayer; Described static flow tank lower openings, join to be communicated with the upper opening of described current stabilization flow tank with described current stabilization flow tank, the bore of the lower openings of described static flow tank is greater than the bore of described reaction chamber upper opening, and described static flow tank is provided with a clear liquid mouth.
Preferably, described back-up ring is the back-up ring that coaxial spaced is arranged.
Preferably, described back-up ring is a reverse frustoconic.
Preferably, described back-up ring is the chamfered edge taper type.
Preferably, described reactant liquor import is arranged on the top of described agitator.
Preferably, also be provided with rinse mouth and discharging hole on the described reaction chamber sidewall.
Preferably, nearly upper opening place also is provided with a sample tap on the sidewall of described reaction chamber.
Preferably, in the oblique insertion reaction chamber of the described agitator sidewall, described agitator is that rotating speed surpasses 250 rev/mins agitator.
Preferably, in the described current stabilization flow tank in the back-up ring of inner ring the also coaxial bubble-cap of falling the infundibulate that is provided with, the top of the described bubble-cap of falling the infundibulate is provided with a circulation pipe, and described circulation pipe one end is communicated with the bubble-cap of falling the infundibulate, and the above the reactant liquor import of the other end and described reaction chamber links to each other.
Preferably, the distance between the described back-up ring is 150-300mm.
Preferably, the distance between the bottom cover edge of the described bubble-cap of falling the infundibulate and the described inner ring back-up ring is 150-300mm.
Preferably, the top of described static flow tank also is provided with a clear liquid groove, and described clear liquid groove communicates with clear liquid mouth on the described static flow tank.
Preferably, the top of described static flow tank also is provided with an overflow launder, and described overflow launder is provided with an overfall.
Preferably, described overflow launder is located at the top of described clear liquid groove.
The invention has the advantages that: homogeneous-phase fluidized bed reactor is the equipment of nationality material reaction and isolation integral, make fluid foods in reaction chamber bottom strenuous exercise, be beneficial to calcium chloride and material liquid fully mixes, reduced the ion concentration of material in mixer attachment, slowed down reaction speed, thus tiny CaSO avoided
4Particle generates and prevents fouling; The CaSO that generated simultaneously
4A particle part is stayed the interior crystal seed as subsequent reactions of reaction chamber, the final CaSO that generates of reaction
4Particle is discharged from slag-drip opening; The clear liquid mouth is discharged the sedimentation coefficient SV30 of clear liquid less than 30%; Satisfying under the process conditions, this homogeneous-phase fluidized bed reactor can make the demand of calcium ion from Ca
2+: SO
4 2-＞2: 1 reduces to Ca
2+: SO
4 2-＞1.5: 1, reduced the cost of production post processing, saved the energy, help the calcium method and remove the popularization of nitre method in caustic soda industry.
Description of drawings
Fig. 1 is the first embodiment schematic diagram of homogeneous-phase fluidized bed reactor structure of the present invention;
Fig. 2 for first embodiment of homogeneous-phase fluidized bed reactor structure of the present invention along A-A line sectional view among Fig. 1;
Fig. 3 for first embodiment of homogeneous-phase fluidized bed reactor structure of the present invention along C-C line sectional view among Fig. 1;
Fig. 4 is the second embodiment schematic diagram of homogeneous-phase fluidized bed reactor structure of the present invention;
Fig. 5 for second embodiment of homogeneous-phase fluidized bed reactor structure of the present invention along A-A line sectional view among Fig. 4;
Fig. 6 for second embodiment of homogeneous-phase fluidized bed reactor structure of the present invention along C-C line sectional view among Fig. 4;
Fig. 7 is the 3rd embodiment schematic diagram of homogeneous-phase fluidized bed reactor structure of the present invention;
Fig. 8 for the 3rd embodiment of homogeneous-phase fluidized bed reactor structure of the present invention along A-A line sectional view among Fig. 7;
Fig. 9 for the 3rd embodiment of homogeneous-phase fluidized bed reactor structure of the present invention along C-C line sectional view among Fig. 7;
Figure 10 is the 4th embodiment schematic diagram of homogeneous-phase fluidized bed reactor structure of the present invention;
Figure 11 for the 4th embodiment of homogeneous-phase fluidized bed reactor structure of the present invention along A-A line sectional view among Figure 10;
Figure 12 for the 4th embodiment of homogeneous-phase fluidized bed reactor structure of the present invention along C-C line sectional view among Figure 10.
The specific embodiment
The present invention is further illustrated below in conjunction with accompanying drawing.
Referring to Fig. 1, Fig. 2 and Fig. 3, shown in the figure the first embodiment schematic diagram of homogeneous-phase fluidized bed reactor structure of the present invention.Comprise that a cylindrical reaction chamber 2, is arranged on cylindrical current stabilization flow tank 3 on the described reaction chamber 2, and one is arranged on bottom bore on the described current stabilization flow tank 3 greater than the cylindrical static flow tank 4 of described reaction chamber 2 upper opening bores; The upper opening of described reaction chamber 2, and join with described current stabilization flow tank 3 and to be communicated with, the sidewall of described reaction chamber 2 is provided with material liquid import 14, reactant liquor import 8 and slag-drip opening 16, along also evenly being laid with two agitators 5 in the sidewall of described reaction chamber 2; Described current stabilization flow tank 3 is equal cavity of opening up and down, and its underpart opening joins to be communicated with described reaction chamber 2 with the upper opening of described reaction chamber 2, and its upper opening joins with described static flow tank 3 and is communicated with; Described current stabilization flow tank 3 is provided with the reverse frustoconic back-up ring 6 that a plurality of spacings are the 150mm arranged in co-axial alignment, described static flow tank 4 lower openings, join to be communicated with described current stabilization flow tank 3 with the upper opening of described current stabilization flow tank 3, described static flow tank 4 is provided with a clear liquid mouth 12.
Material liquid adds in the described reaction chamber 2 from described reactant liquor import 8 from material liquid import 14, the reactant liquor of reaction chamber 2, described agitator 5 stirs with 250 rev/mins speed, reduce material liquid and near the concentration of reactant liquor material liquid import 14 and reactant liquor import 8 rapidly, make material liquid, reactant liquor mix the formation mixed liquor rapidly, reaction generates CaSO
4Particle; Under the prolonged agitation of described agitator 5, and along with the increasing gradually of material liquid that adds and reactant liquor, the mixed liquor in the described reaction chamber 2 is stable to enter described current stabilization flow tank 3 constantly.
When mixed liquor enters current stabilization flow tank 3, the CaSO in the mixed liquor
4Particle is stopped by back-up ring 6, has slowed down CaSO
4The speed that particle rises, most CaSO
4Particle is blocked back to slide in the described reaction chamber 2 and continues to grow up, and directly only becomes oarse-grained deposit seed.
Mixed liquor after the stopping of current stabilization flow tank 3 guide rings 6, wherein contained CaSO
4Amounts of particles significantly reduces, and the mixed liquor movement velocity is also slowed down, and with the increasing of the material in the described reaction chamber 2, the mixed liquor in the current stabilization flow tank 3 continues the stable static flow tank 4 that enters constantly; In static flow tank 4, because the bore of static flow tank 4 lower openings is greater than the bore of described reaction chamber 2 upper openings, the movement velocity of mixed liquor reduces gradually, simultaneously, the mixed liquor liquid level slowly rises in static flow tank 4, mixed liquor is able to carry out sedimentation under stable state, wherein surplus CaSO
4Particle is got back in the reaction chamber 2 through 3 sedimentations of current stabilization flow tank because of gravity, and the supernatant liquor of mixed liquor is discharged homogeneous-phase fluidized bed reactor 1 through described clear liquid mouth 12 in the static flow tank 4.Most CaSO in the reaction chamber 2
4Deposit seed is discharged from the slag-drip opening 16 of reaction chamber 2, a small amount of CaSO
4Particle can be stayed in the reaction chamber 2 crystal seed as subsequent reactions.
Referring to Fig. 4, Fig. 5 and Fig. 6, shown in the figure the second embodiment schematic diagram of homogeneous-phase fluidized bed reactor structure of the present invention.Comprise that a prismatic reaction chamber 2, is arranged on the cylindrical current stabilization flow tank 3 on the described reaction chamber 2, and one is arranged on the described current stabilization flow tank 3 the bottom bore greater than the square static flow tank 4 of described reaction chamber 2 upper opening bores; The upper opening of described reaction chamber 2, and join with described current stabilization flow tank 3 and to be communicated with, the sidewall of described reaction chamber 2 is provided with that nearly its upper opening place also is provided with a sample tap 13 on the sidewall of material liquid import 14, reactant liquor import 8, slag-drip opening 16 and described reaction chamber 2, along also evenly being laid with four agitators 5 in the sidewall of described reaction chamber 2, the central shaft of described agitator 5 all tilts by certain angle; Described current stabilization flow tank 3 is equal cavity of opening up and down, its underpart opening joins to be communicated with described reaction chamber 2 with the upper opening of described reaction chamber 2, its upper opening joins with described static flow tank 3 and is communicated with, described current stabilization flow tank 3 is provided with the reverse frustoconic back-up ring 6 that a plurality of spacings are the 200mm arranged in co-axial alignment, described inner ring reverse frustoconic back-up ring 6 also is provided with a bubble-cap of falling the infundibulate 7, spacing between the bottom cover edge of described bubble-cap 7 and the described inner ring reverse frustoconic back-up ring 6 is 200mm, the top of the described bubble-cap of falling the infundibulate 7 also is provided with a circulation pipe 8, described circulation pipe 8 one ends are communicated with turbination bubble-cap 7, and the other end stretches out the outer wall of described homogeneous-phase fluidized bed reactor 1; Described static flow tank 4 lower openings are joined to be communicated with described current stabilization flow tank 3 with the upper opening of described current stabilization flow tank 3, and the top of described static flow tank 4 also is provided with a clear liquid groove 11, and described clear liquid groove 11 is provided with a clear liquid mouth 12.
Material liquid enters in the described reaction chamber 2 from described reactant liquor import 8 from material liquid import 14, the reactant liquor of reaction chamber 2, described four agitators 5 acutely turn round with 270 rev/mins speed, reduce material liquid and near the concentration of reactant liquor material liquid import 14 and reactant liquor import 8 rapidly, make material liquid, reactant liquor mix the formation mixed liquor rapidly, reaction generates CaSO
4Particle; Reaction is carried out in the process, detects the situation of carrying out of tracking reaction from sample tap 13 samplings of reaction chamber 2 sidewalls; Under the prolonged agitation of described agitator 5, and along with the increasing gradually of material liquid that adds and reactant liquor, the mixed liquor in the described reaction chamber 2 is stable to enter described current stabilization flow tank 3 constantly.
When mixed liquor enters current stabilization flow tank 3, the CaSO in the mixed liquor
4Particle is stopped by back-up ring 6 and bubble-cap 7, slowed down the speed that particle rises, most particles are blocked back and slide in the described reaction chamber 2, the mixed liquor that is stopped by bubble-cap 7 evenly goes back to the periphery of cloth to described reaction chamber 2 along the surface of back-up ring 6, help the dispersion of mixed liquor, thereby what help reacting proceeds, the mixed liquor that small part enters bubble-cap 7 tops is located at the circulation port 10 at top through it, quantitatively mixed liquor is discharged, enter continuation reaction in the described reaction chamber 2 from material liquid import 8, with this speed of slowing down reaction, make CaSO
4Particle continues to grow up, and directly only becomes oarse-grained deposit seed.
Mixed liquor after back-up ring 6 in current stabilization flow tank 3 and bubble-cap 7 stop, wherein contained CaSO
4Amounts of particles significantly reduces, and the movement velocity of mixed liquor is slowed down, and with the increasing of the material in the described reactor 1, the mixed liquor in the current stabilization flow tank 3 continues the stable static flow tank 4 that enters constantly; In static flow tank 4, because the bore of the lower openings of static flow tank 4 is greater than the bore of described reaction chamber 2 upper openings, the movement velocity of mixed liquor reduces gradually, simultaneously, the mixed liquor liquid level slowly rises in static flow tank 4, mixed liquor is able to carry out sedimentation under stable state, wherein surplus CaSO
4Particle is got back in the reaction chamber 2 through 3 sedimentations of current stabilization flow tank because of gravity, and the supernatant liquor of mixed liquor is discharged homogeneous-phase fluidized bed reactor 1 along the clear liquid mouth on the clear liquid groove 11 12 in the static flow tank 4.Most CaSO in the reaction chamber 2
4Deposit seed is discharged from the slag-drip opening 16 of reaction chamber 2, a small amount of CaSO
4Particle can be stayed in the reaction chamber 2 crystal seed as subsequent reactions.
Referring to Fig. 7, Fig. 8 and Fig. 9, shown in the figure the 3rd embodiment schematic diagram of homogeneous-phase fluidized bed reactor structure of the present invention.Comprise that a cylindrical reaction chamber 2, is arranged on the polygon current stabilization flow tank 3 on the described reaction chamber 2, and one is arranged on bottom bore on the described current stabilization flow tank 3 greater than the cylindrical static flow tank 4 of described reaction chamber 2 upper opening bores; The upper opening of described reaction chamber 2, and join with described current stabilization flow tank 3 and to be communicated with, the sidewall of described reaction chamber 2 is provided with that nearly its upper opening place also is provided with a sample tap 13 on the sidewall of material liquid import 14, reactant liquor import 8, rinse mouth 9, discharging hole 10, slag-drip opening 16 and described reaction chamber 2, along also evenly being laid with four agitators 5 in the sidewall of described reaction chamber 2, the central shaft of described agitator 5 tilts by certain angle, described rinse mouth 9 be located at described agitator 51 above, described discharging hole 10 is located at described agitator 52 below; Described current stabilization flow tank 3 is equal cavity of opening up and down, its underpart opening joins to be communicated with described reaction chamber 2 with the upper opening of described reaction chamber 2, its upper opening joins with described static flow tank 3 and is communicated with, described current stabilization flow tank 3 is provided with the chamfered edge taper type back-up ring 6 that a plurality of spacings are the 300mm arranged in co-axial alignment, described inner ring chamfered edge taper type back-up ring 6 also is provided with a bubble-cap of falling the infundibulate 7, spacing between the bottom cover edge of described bubble-cap 7 and the described inner ring chamfered edge taper type back-up ring 6 is 300mm, the top of the described bubble-cap of falling the infundibulate 7 also is provided with a circulation pipe 8, described circulation pipe 8 one ends are communicated with the bubble-cap of falling the infundibulate 7, and the other end stretches out the outer wall of described homogeneous-phase fluidized bed reactor 1; Described static flow tank 4 lower openings, join to be communicated with the upper opening of described current stabilization flow tank 3 with described current stabilization flow tank 3, the top of described static flow tank 4 also is provided with a clear liquid groove 11, described clear liquid groove 11 is provided with a clear liquid mouth 12, the top of described static flow tank 4 also has an overflow launder 17, and described overflow launder 17 is provided with an overfall 15.
Material liquid enters in the described reaction chamber 2 from described reactant liquor import 8 from material liquid import 14, the reactant liquor of reaction chamber 2, described four agitators 5 are with 300 rev/mins speed vigorous stirring, reduce material liquid and near the concentration of reactant liquor material liquid import 14 and reactant liquor import 8 rapidly, make material liquid, reactant liquor mix the formation mixed liquor rapidly, reaction generates CaSO
4Particle; Reaction is carried out in the process, detects the situation of carrying out of tracking reaction from sample tap 13 samplings of reaction chamber 2 sidewalls; Under the prolonged agitation of described agitator 5, and along with the increasing gradually of material liquid that adds and reactant liquor, the mixed liquor in the described reaction chamber 2 is stable to enter described current stabilization flow tank 3 constantly.
When mixed liquor enters current stabilization flow tank 3, the CaSO in the mixed liquor
4Particle is stopped by back-up ring 6 and bubble-cap 7, has slowed down the speed that particle rises, most CaSO
4Particle is blocked back and slides in the described reaction chamber 2, the mixed liquor that stops through bubble-cap 7 evenly goes back to the periphery of cloth to described reaction chamber 2 along the surface of back-up ring 6, help the dispersion of mixed liquor, thereby what help reacting proceeds, the mixed liquor that enters bubble-cap 7 is located at the circulation port 10 at top through it, quantitatively mixed liquor is discharged, and enters from material liquid import 8 and continues reaction in the described reaction chamber 2, with this speed of slowing down reaction, make CaSO
4Particle continues to grow up, and directly only becomes oarse-grained deposit seed.
Mixed liquor after back-up ring 6 in current stabilization flow tank 3 and bubble-cap 7 stop, wherein contained CaSO
4Amounts of particles significantly reduces, and the movement velocity of mixed liquor is slowed down, and with the increasing of the material in the described reactor 1, the mixed liquor in the current stabilization flow tank 3 continues the stable static flow tank 4 that enters constantly; Because the bore of the lower openings of static flow tank 4 is greater than the bore of described reaction chamber 2 upper openings, the movement velocity of mixed liquor reduces gradually, and simultaneously, the mixed liquor liquid level slowly rises in static flow tank 4, mixed liquor is able to carry out sedimentation under stable state, wherein surplus CaSO
4Particle is got back in the reaction chamber 2 through 3 sedimentations of current stabilization flow tank because of gravity, the supernatant liquor of mixed liquor is discharged homogeneous-phase fluidized bed reactor 1 along the clear liquid mouth on the clear liquid groove 11 12 in the static flow tank 4, when the clear liquid amount was big, supernatant liquor was discharged homogeneous-phase fluidized bed reactor 1 along overflow launder 17 through overfall 15.Most CaSO in the reaction chamber 2
4Particle is discharged from the slag-drip opening 16 of reaction chamber 2, a small amount of CaSO
4Particle can be stayed in the reaction chamber 2 crystal seed as subsequent reactions.
When described reaction chamber 2 cleaned, clear water was squeezed into from the rinse mouth 9 of reaction chamber 2 sidewalls, and sewage is discharged from the discharging hole 10 of described reaction chamber 2 sidewalls.
Referring to Figure 10, Figure 11 and Figure 12, shown in the figure the 4th embodiment schematic diagram of homogeneous-phase fluidized bed reactor structure of the present invention.Comprise that a square reaction chamber 2, is arranged on the square current stabilization flow tank 3 on the described reaction chamber 2, and one is arranged on bottom bore on the described current stabilization flow tank 3 greater than the square static flow tank 4 of described reaction chamber 2 upper opening bores; The upper opening of described reaction chamber 2, and join with described current stabilization flow tank 3 and to be communicated with, the sidewall of described reaction chamber 2 is provided with material liquid import 14, reactant liquor import 8 and slag-drip opening 16, along also evenly being laid with four agitators 5 in the sidewall of described reaction chamber 2, the central shaft of described agitator 5 tilts by certain angle; Described current stabilization flow tank 3 is equal cavity of opening up and down, its underpart opening joins to be communicated with described reaction chamber 2 with the upper opening of described reaction chamber 2, its upper opening joins with described static flow tank 4 and is communicated with, and described current stabilization flow tank 3 is provided with the square back-up ring 6 that a plurality of spacings are the equidirectional arrangement of 250mm; Described static flow tank 4 lower openings are joined to be communicated with described current stabilization flow tank 3 with the upper opening of described current stabilization flow tank 3, and the top of described static flow tank 4 also is provided with a clear liquid groove 11, and described clear liquid groove 11 is provided with a clear liquid mouth 12.
Material liquid enters in the described reaction chamber 2 from described reactant liquor import 8 from material liquid import 14, the reactant liquor of reaction chamber 2, described four agitators 5 are with 300 rev/mins speed vigorous stirring, reduce material liquid and near the concentration of reactant liquor material liquid import 14 and reactant liquor import 8 rapidly, make material liquid, reactant liquor mix the formation mixed liquor rapidly, reaction generates CaSO
4Particle; Under the prolonged agitation of described agitator 5, and along with the increasing gradually of material liquid that adds and reactant liquor, the mixed liquor in the described reaction chamber 2 is stable to enter described current stabilization flow tank 3 constantly.
When mixed liquor enters current stabilization flow tank 3, the CaSO in the mixed liquor
4Particle has been slowed down the speed that particle rises, most CaSO by back-up ring 6
4Particle is blocked back and slides in the described reaction chamber 2, continues reaction, makes CaSO
4Particle continues to grow up, and directly only becomes oarse-grained deposit seed.
Mixed liquor after back-up ring 6 in current stabilization flow tank 3 stops, wherein contained CaSO
4Amounts of particles significantly reduces, and the movement velocity of mixed liquor is slowed down, and with the increasing of the material in the described reactor 1, the mixed liquor in the current stabilization flow tank 3 continues the stable static flow tank 4 that enters constantly; Because no longer being subjected to external force, stirs the mixed liquor in the static flow tank 4, the movement velocity of mixed liquor reduces gradually, simultaneously, because the bore of the lower openings of static flow tank 4 is greater than the bore of described reaction chamber 2 upper openings, the mixed liquor liquid level slowly rises in static flow tank 4, mixed liquor is able to carry out sedimentation under stable state, wherein surplus CaSO
4Particle is got back in the reaction chamber 2 through 3 sedimentations of current stabilization flow tank because of gravity, and the supernatant liquor of mixed liquor is discharged homogeneous-phase fluidized bed reactor 1 along clear liquid groove 11 from clear liquid mouth 12 in the static flow tank 4.Most CaSO in the reaction chamber 2
4Particle is discharged from the slag-drip opening 16 of reaction chamber 2, a small amount of CaSO
4Particle can be stayed in the reaction chamber 2 crystal seed as subsequent reactions.
From the above as seen, homogeneous-phase fluidized bed reactor of the present invention can be removed the sulfate radical that accumulates in the production of caustic soda effectively and prevent CaSO
4Generate tiny particle and fouling, make reaction reach balance, SO simultaneously at a certain temperature
4 2-Ion obtains maximum precipitation, through practice, utilizes this homogeneous-phase fluidized bed reactor, and the molar concentration rate of required calcium ion can reduce to Ca
2+: SO
4 2-＞1.5: 1.
Above-described embodiment is several implementation of the present invention; but protection scope of the present invention is not limited to the specific descriptions in the foregoing description; all by the present invention design to conversion that the above embodiment does; being such as but not limited to described reaction chamber 2 also can be prism shape etc., all within the scope of the invention.
Claims (14)
1. homogeneous-phase fluidized bed reactor, comprise a reaction chamber, the sidewall of described reaction chamber is provided with material liquid import, reactant liquor import and slag-drip opening, it is characterized in that, described homogeneous-phase fluidized bed reactor comprises that also one is arranged on the current stabilization flow tank on the described reaction chamber, and a static flow tank that is arranged on the described current stabilization flow tank; The upper opening of described reaction chamber, and join with described current stabilization flow tank and to be communicated with, along also evenly being laid with plural agitator in the sidewall of described reaction chamber; Described current stabilization flow tank is equal cavity of opening up and down, its underpart opening joins with the upper opening of described reaction chamber and is communicated with described reaction chamber, its upper opening joins with described static flow tank and is communicated with, and described current stabilization flow tank comprises the spaced back-up ring of multilayer; Described static flow tank lower openings, join with the upper opening of described current stabilization flow tank and be communicated with described current stabilization flow tank, the bore of the lower openings of described static flow tank is greater than the bore of described reaction chamber upper opening, and described static flow tank is provided with a clear liquid mouth.
2. a kind of homogeneous-phase fluidized bed reactor as claimed in claim 1 is characterized in that, described back-up ring is the back-up ring that coaxial spaced is arranged.
3. a kind of homogeneous-phase fluidized bed reactor as claimed in claim 1 is characterized in that, described back-up ring is a reverse frustoconic.
4. a kind of homogeneous-phase fluidized bed reactor as claimed in claim 1 is characterized in that, described back-up ring is the chamfered edge taper type.
5. a kind of homogeneous-phase fluidized bed reactor as claimed in claim 1 is characterized in that described reactant liquor import is arranged on the top of described agitator.
6. a kind of homogeneous-phase fluidized bed reactor as claimed in claim 1 is characterized in that, also is provided with rinse mouth and discharging hole on the described reaction chamber sidewall.
7. a kind of homogeneous-phase fluidized bed reactor as claimed in claim 1 is characterized in that, nearly upper opening place also is provided with a sample tap on the sidewall of described reaction chamber.
8. a kind of homogeneous-phase fluidized bed reactor as claimed in claim 1 is characterized in that, in the oblique insertion reaction chamber of the described agitator sidewall, described agitator is that rotating speed surpasses 250 rev/mins agitator.
9. a kind of homogeneous-phase fluidized bed reactor as claimed in claim 1, it is characterized in that, in the described current stabilization flow tank in the back-up ring of inner ring the also coaxial bubble-cap of falling the infundibulate that is provided with, the top of the described bubble-cap of falling the infundibulate is provided with a circulation pipe, described circulation pipe one end is communicated with the bubble-cap of falling the infundibulate, and the above the reactant liquor import of the other end and described reaction chamber links to each other.
10. a kind of homogeneous-phase fluidized bed reactor as claimed in claim 1 is characterized in that, the distance between the described back-up ring is 150-300mm.
11. a kind of homogeneous-phase fluidized bed reactor as claimed in claim 9 is characterized in that, the distance between the bottom cover edge of the described bubble-cap of falling the infundibulate and the described inner ring back-up ring is 150-300mm.
12 a kind of homogeneous-phase fluidized bed reactors as claimed in claim 1 is characterized in that the top of described static flow tank also is provided with a clear liquid groove, and described clear liquid groove communicates with clear liquid mouth on the described static flow tank.
13. a kind of homogeneous-phase fluidized bed reactor as claimed in claim 12 is characterized in that the top of described static flow tank also is provided with an overflow launder, described overflow launder is provided with an overfall.
14. a kind of homogeneous-phase fluidized bed reactor as claimed in claim 13 is characterized in that described overflow launder is located at the top of described clear liquid groove.
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| Application Number | Priority Date | Filing Date | Title |
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| CNB2005100249617A CN100358623C (en) | 2005-04-07 | 2005-04-07 | Homogeneous-phase fluidized bed reactor |
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| CNB2005100249617A CN100358623C (en) | 2005-04-07 | 2005-04-07 | Homogeneous-phase fluidized bed reactor |
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| CN1843609A CN1843609A (en) | 2006-10-11 |
| CN100358623C true CN100358623C (en) | 2008-01-02 |
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| CNB2005100249617A Active CN100358623C (en) | 2005-04-07 | 2005-04-07 | Homogeneous-phase fluidized bed reactor |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4087253A (en) * | 1975-03-28 | 1978-05-02 | Rhone-Poulenc Industries | Method of obtaining caustic soda from a sodium chloride liquor containing sulphate ions recovered from an electrolytic cell |
| US4565612A (en) * | 1984-12-10 | 1986-01-21 | The Dow Chemical Company | Process for reducing sulphate ion concentration in aqueous sodium hydroxide solutions |
| CN1039781A (en) * | 1989-06-17 | 1990-02-21 | 自贡市张家坝制盐化工厂 | A kind of method that purifies sodium chloride brine and bittern |
| CN1169397A (en) * | 1996-06-26 | 1998-01-07 | 李运生 | Ternary brine denitration liquid |
| CN1403373A (en) * | 2002-09-20 | 2003-03-19 | 南化集团设计院 | Sulfate radical-eliminating process for underground bittern |
| CN2775029Y (en) * | 2005-04-07 | 2006-04-26 | 凯膜过滤技术(上海)有限公司 | Homogeneous phase fluidized bed reactor |
-
2005
- 2005-04-07 CN CNB2005100249617A patent/CN100358623C/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4087253A (en) * | 1975-03-28 | 1978-05-02 | Rhone-Poulenc Industries | Method of obtaining caustic soda from a sodium chloride liquor containing sulphate ions recovered from an electrolytic cell |
| US4565612A (en) * | 1984-12-10 | 1986-01-21 | The Dow Chemical Company | Process for reducing sulphate ion concentration in aqueous sodium hydroxide solutions |
| CN1039781A (en) * | 1989-06-17 | 1990-02-21 | 自贡市张家坝制盐化工厂 | A kind of method that purifies sodium chloride brine and bittern |
| CN1169397A (en) * | 1996-06-26 | 1998-01-07 | 李运生 | Ternary brine denitration liquid |
| CN1403373A (en) * | 2002-09-20 | 2003-03-19 | 南化集团设计院 | Sulfate radical-eliminating process for underground bittern |
| CN2775029Y (en) * | 2005-04-07 | 2006-04-26 | 凯膜过滤技术(上海)有限公司 | Homogeneous phase fluidized bed reactor |
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|---|---|
| CN1843609A (en) | 2006-10-11 |
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