CN1843609A - Homogeneous-phase fluidized bed reactor - Google Patents
Homogeneous-phase fluidized bed reactor Download PDFInfo
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- CN1843609A CN1843609A CN200510024961.7A CN200510024961A CN1843609A CN 1843609 A CN1843609 A CN 1843609A CN 200510024961 A CN200510024961 A CN 200510024961A CN 1843609 A CN1843609 A CN 1843609A
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Abstract
The invention relates to a monophasic fluid bed reactor, which comprises a reaction box whose side wall has a inlet of raw material, a inlet of reaction liquid and a outlet of slag; a tranquilling depositing tank above the reaction box; and a static depositing tank above the tranquilling depositing tank. Wherein, the upper outlet of reaction box is through to the tranquilling depositing tank and at least two mixer are uniformly distributed on its side wall; the tranquilling depositing tank is a chamber with upper and lower opens, while the lower one is through to the reaction box and the upper one is through to the static depositing tank, and it comprises several layers of baffle rings; the lower outlet of static depositing tank is through to the upper outlet of tranquilling depositing tank and the diameter of lower outlet is larger that the upper outlet of reaction box, while said static depositing tank has a clear liquid open. Said monophasic fluid bed reactor can avoid small calcium sulphate, while the mol concentration of needed calcium ion is reduced as Ca2+:SO42->1.5:1, to reduce the cost and energy consumption.
Description
Technical Field
The invention relates to a continuous reactor, in particular to a homogeneous phase fluidized bed reactor for removing sulfate radicals in caustic soda production by adopting a calcium method.
Background
The caustic soda is used as an important industrial material, is widely applied to the fields of papermaking, daily washing and light industry, and especially plays an important role in the fields of petrochemical industry (chemical and medical industry, glass, enamel, leather making and food production). In China, a plurality of manufacturers use high-mango brine to prepare caustic soda, and sulfate radicals generated in the production are generated in the whole process along with the increase of the yield of the caustic soda, particularly the yield of high-concentration liquid caustic soda and ion membrane caustic soda of a diaphragmThe more the product is accumulated in the system, the more the product is difficult to treat, the normal operation of caustic soda equipment is restricted, and the adverse effect on normal production is caused. For the treatment of sulfate radicals, China basically adopts a barium method to remove the nitrate, and a few manufacturers adopt a calcium method to remove the nitrate. Relatively speaking, although the barium method has a good nitrate removal effect, the required cost is high, the generated barium sulfate is difficult to settle and separate, the residual barium ions in the secondary refined brine are easy to exceed the standard, and the barium ions are toxic and can cause harm to the health of production personnel; at present, CaCl is adopted for removing nitrate by the calcium method2With SO4 2-Reaction to produce CaSO4Precipitating (I), filtering to obtain CaSO4Theprecipitate is filtered from the brine, thereby removing sulfuric acid
Disclosure of Invention
One of the purposes of the invention is to provide a method for removing sulfate radical accumulated in caustic soda production by adopting a calcium method and preventing CaSO4Forming fine particles to form scale, and balancing the reaction at a certain temperature to obtain SO4 2-Of the calcium ions required under the conditions of the precipitation process in which the ions are maximally obtainedThe molar concentration ratio is reduced to Ca2+∶SO4 2-A homogeneous phase flow bed reactor with the ratio of more than 1.5: 1.
In order to achieve the above object, the present invention provides a homogeneous phase flow bed reactor, comprising 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 discharge port, and the homogeneous phase flow bed reactor is characterized by further comprising a steady flow settling box arranged above the reaction box, and a static settling box arranged above the steady flow settling box; the upper part of the reaction box is opened and is connected and communicated with the steady flow settling box, and two or more than two stirrers are uniformly distributed in the side wall of the reaction box; the steady flow settling tank is a cavity with openings at the upper part and the lower part, the opening at the lower part of the steady flow settling tank is connected with the opening at the upper part of the reaction tank so as to be communicated with the reaction tank, the opening at the upper part of the steady flow settling tank is connected and communicated with the static settling tank, and the steady flow settling tank comprises a plurality of layers of check rings which are arranged at intervals; the lower opening of the static settling tank is connected with the upper opening of the steady flow settling tank so as to be communicated with the steady flow settling tank, the caliber of the lower opening of the static settling tank is larger than that of the upper opening of the reaction tank, and the static settling tank is provided with a clear liquid port.
Preferably, the retainer rings are coaxially arranged at intervals.
Preferably, the retainer ring is in the shape of an inverted truncated cone.
Preferably, the retainer ring is in a shape of a truncated pyramid.
Preferably, the reaction liquid inlet is disposed above the stirrer.
Preferably, the side wall of the reaction box is also provided with a flushing port and a draining port.
Preferably, a sampling port is further disposed on the sidewall of the reaction chamber near the upper opening.
Preferably, the stirrer is obliquely inserted into the side wall of the reaction box, and the stirrer is a stirrer rotating at a speed of more than 250 revolutions per minute.
Preferably, an inverted funnel-shaped bubble cap is coaxially arranged in the retaining ring at the innermost ring in the steady-flow settling tank, a circulating pipe is arranged at the top of the inverted funnel-shaped bubble cap, one end of the circulating pipe is communicated with the inverted funnel-shaped bubble cap, and the other end of the circulating pipe is connected with the reaction liquid inlet on the reaction tank.
Preferably, the distance between the retaining rings is 150-300 mm.
Preferably, the distance between the bottom cover edge of the inverted funnel-shaped bubble cap and the innermost ring retainer ring is 150mm and 300 mm.
Preferably, the upper part of the static settling tank is further provided with a clear liquid groove, and the clear liquid groove is communicated with a clear liquid port on the static settling tank.
Preferably, the upper part of the static settling tank is further provided with an overflow trough, and the overflow trough is provided with an overflow port.
Preferably, the overflow groove is arranged at the upper part of the clear liquid groove.
The invention has the advantages that: the homogeneous phase flow bed reactor is a device integrating material reaction and separation, which ensures that fluid materials move violently at the bottom of the reaction tank, is beneficial to fully mixing calcium chloride and raw material liquid, reduces the ion concentration of the materials at the accessory of a stirrer, and slows down the reaction speed, thereby avoiding the situation that the fine CaSO is generated4Particle generation prevents fouling; with previously generated CaSO4Part of the particles are left in the reaction box to be used as seed crystals for subsequent reaction, and CaSO finally generated by the reaction4Discharging the particles from a slag discharge port; the sedimentation coefficient SV30 of the clear liquid discharged from the clear liquid port is less than 30 percent; under the condition of meeting the process conditions, the homogeneous phase fluidized bed reactor can ensure that the required amount of calcium ions is increased from Ca2+∶SO4 2-Reduction to Ca>2: 12+∶SO4 2-More than 1.5: 1, reduces the cost of post-treatment of production and saves energyThe source is beneficial to the popularization of the calcium method denitration method in the caustic soda industry.
Drawings
FIG. 1 is a schematic view of a first embodiment of a homogeneous flow bed reactor configuration according to the present invention;
FIG. 2 is a sectional view of a first embodiment of a homogeneous phase flow bed reactor configuration of the present invention taken along line A-A of FIG. 1;
FIG. 3 is a sectional view of a first embodiment of a homogeneous flow bed reactor configuration according to the present invention taken along line C-C of FIG. 1;
FIG. 4 is a schematic view of a second embodiment of a homogeneous flow bed reactor configuration according to the present invention;
FIG. 5 is a sectional view taken along line A-A in FIG. 4 of a second embodiment of a homogeneous phase flow bed reactor configuration according to the present invention;
FIG. 6 is a sectional view of a second embodiment of a homogeneous flow bed reactor configuration according to the present invention taken along line C-C of FIG. 4;
FIG. 7 is a schematic view of a third embodiment of a homogeneous flow bed reactor configuration according to the present invention;
FIG. 8 is a sectional view of a third embodiment of a homogeneous flow bed reactor configuration according to the present invention taken along line A-A in FIG. 7;
FIG. 9 is a sectional view of a third embodiment of a homogeneous flow bed reactor configuration according to the present invention taken along line C-C of FIG. 7;
FIG. 10 is a schematic view of a fourth embodiment of a homogeneous flow bed reactor configuration according to the present invention;
FIG. 11 is a sectional view taken along line A-A in FIG. 10 of a fourth embodiment of a homogeneous phase flow bed reactor configuration according to the present invention;
FIG. 12 is a sectional view of a fourth embodiment of the structure of the homogeneous flow bed reactor of the present invention taken along line C-C of FIG. 10.
Detailed Description
The invention will be further described with reference to the accompanying drawings.
Referring to fig. 1, 2 and 3, there is shown a schematic diagram of a first embodiment of a homogeneous phase flow bed reactor configuration of the present invention. The device comprises a cylindrical reaction box 2, a cylindrical steady flow settling box 3 arranged above the reaction box 2, and a cylindrical static settling box 4 which is arranged above the steady flow settling box 3 and has the caliber of the lower part larger than the caliber of an opening at the upper part of the reaction box 2; the upper part of the reaction box 2 is opened and is connected and communicated with the steady flow settling box 3, the side wall of the reaction box 2 is provided with a raw material liquid inlet 14, a reaction liquid inlet 8 and a slag discharge port 16, and two stirrers 5 are uniformly distributed in the side wall of the reaction box 2; the steady flow settling tank 3 is a cavity with openings at the upper and lower parts, the opening at the lower part is connected with the opening at the upper part of the reaction tank 2 so as to be communicated with the reaction tank 2, and the opening at the upper part is connected and communicated with the static settling tank 3; the steady flow settling tank 3 is provided with a plurality of reverse circular truncated cone-shaped check rings 6 which are coaxially arranged at intervals of 150mm, the lower opening of the static settling tank 4 is connected with the upper opening of the steady flow settling tank 3 so as to be communicated with the steady flow settling tank 3, and the static settling tank 4 is provided with a clear liquid port 12.
The raw material liquid is added into the reaction box 2 from the raw material liquid inlet 14 of the reaction box 2 and the reaction liquid from the reaction liquid inlet 8, the stirrer 5 is used for stirring at the speed of 250 revolutions per minute, the concentration of the raw material liquid and the concentration of the reaction liquid near the raw material liquid inlet 14 and the reaction liquid inlet 8 are rapidly reduced, the raw material liquid and the reaction liquid are rapidly and uniformly mixed to form a mixed liquid, and CaSO is generated through reaction4Particles; under the continuous agitation of said stirrer 5,and the mixed liquid in the reaction box 2 stably and continuously enters the steady flow settling box 3 along with the gradual increase of the added raw material liquid and the added reaction liquid.
When the mixed liquid enters the steady flow settling tank 3, the CaSO in the mixed liquid4The particles are blocked by the retaining ring 6, thereby slowing down CaSO4Rate of particle ascent, most CaSO4The particles are blocked from sliding back into the reaction chamber 2 and continue to grow until they become large-grained settled particles.
The mixture liquid after being blocked by a check ring 6 in the steady flow settling tank 3 contains CaSO4The number of particles is greatly reduced, the movement speed of the mixed liquor is also slowed down, and the mixed liquor in the steady flow settling tank 3 continuously and stably enters the static settling tank 4 along with the increase of substances in the reaction tank 2; in the static settling tank 4, because the aperture of the lower opening of the static settling tank 4 is larger than the aperture of the upper opening of the reaction tank 2, the moving speed of the mixed liquor is gradually reduced, meanwhile, the liquid level of the mixed liquor slowly rises in the static settling tank 4, the mixed liquor can be settled in a stable state, and the rest CaSO4The particles are settled back to the reaction box 2 through the steady flow settling box 3 due to gravity, and supernatant of the mixed liquid in the static settling box 4 is discharged out of the homogeneous fluidized bed through the clear liquid port 12A reactor 1. Most of the CaSO in the reaction chamber 24The precipitated particles are discharged from a slag discharge port 16 of the reaction box 2, and a small amount of CaSO4The particles may remain in thereaction chamber 2 as seeds for subsequent reactions.
Referring to fig. 4, 5 and 6, there is shown a schematic diagram of a second embodiment of a homogeneous phase flow bed reactor configuration of the present invention. The device comprises a prismatic reaction box 2, a cylindrical steady flow settling box 3 arranged above the reaction box 2, and a square static settling box 4 which is arranged above the steady flow settling box 3 and has the caliber larger than the caliber of an opening at the upper part of the reaction box 2; the upper part of the reaction box 2 is provided with an opening and is connected and communicated with the steady flow settling box 3, the side wall of the reaction box 2 is provided with a raw material liquid inlet 14, a reaction liquid inlet 8 and a slag discharge port 16, a sampling port 13 is also arranged on the side wall of the reaction box 2 near the upper opening thereof, four stirrers 5 are uniformly distributed in the side wall of the reaction box 2, and the central shafts of the stirrers 5 are inclined at a certain angle; the steady flow settling tank 3 is a cavity with openings at the upper and lower parts, the opening at the lower part is connected with the opening at the upper part of the reaction tank 2 so as to be communicated with the reaction tank 2, the opening at the upper part is connected and communicated with the static settling tank 3, the steady flow settling tank 3 is provided with a plurality of inverted frustum-shaped check rings 6 which are coaxially arranged at the interval of 200mm, the inverted funnel-shaped check ring 6 is also provided with an inverted funnel-shaped bubble cap 7, the interval between the bottom cover edge of the bubble cap 7 and the inverted frustum-shaped check ring 6 at the innermost part is 200mm, the top of the inverted funnel-shaped bubble cap 7 is also provided with a circulating pipe 8, one end of the circulating pipe 8 is communicated with the inverted cone-shaped bubble cap 7, and the other endextends out of the outer; the lower opening of the static settling tank 4 is connected with the upper opening of the steady flow settling tank 3 so as to be communicated with the steady flow settling tank 3, the upper part of the static settling tank 4 is also provided with a clear liquid groove 11, and the clear liquid groove 11 is provided with a clear liquid opening 12.
The raw material liquid is introduced into the reaction tank 2 from the raw material liquid inlet 14 of the reaction tank 2 and the reaction liquid from the reaction liquid inlet 8, and the four stirrers 5 are vigorously operated at a speed of 270 rpm to rapidly reduce the concentrations of the raw material liquid and the reaction liquid in the vicinity of the raw material liquid inlet 14 and the reaction liquid inlet 8, thereby allowing the raw material liquid to flow into the reaction tank 2,The reaction solution is quickly and uniformly mixed to form a mixed solution, and CaSO is generated by reaction4Particles; in the reaction process, sampling from a sampling port 13 on the side wall of the reaction box 2 to detect and track the reaction progress; at the holder of the stirrer 5The stirring is continued, and the mixed liquid in the reaction box 2 stably and continuously enters the steady flow settling box 3 along with the gradual increase of the added raw material liquid and the added reaction liquid.
When the mixed liquid enters the steady flow settling tank 3, the CaSO in the mixed liquid4The particles are blocked by the retainer ring 6 and the bubble cap 7, the rising speed of the particles is slowed down, most of the particles are blocked to slide back into the reaction box 2, the mixed liquid blocked by the bubble cap 7 is uniformly distributed back to the periphery of the reaction box 2 along the surface of the retainer ring 6, the dispersion of the mixed liquid is facilitated, the reaction is facilitated to continue, a small part of the mixed liquid entering the upper part of the bubble cap 7 quantitatively discharges the mixed liquid through the circulating port 10 arranged at the top of the mixed liquid, and the mixed liquid enters the reaction box 2 from the raw material liquid inlet 8 to continue to react, so that the reaction speed is slowed down, and the CaSO is enabled to be4The particles continue to grow until they become large-grained precipitate particles.
The mixed liquid after being blocked by a retainer ring 6 and a bubble cap 7 in the steady flow settling tank 3 contains CaSO4The number of particles is greatly reduced, the movement speed of the mixed liquor is slowed down, and the mixed liquor in the steady flow settling tank 3 continues to stably and continuously enter the static settling tank 4 along with the increase of substances in the reactor 1; in the static settling tank 4, because the aperture of the lower opening of the static settling tank 4 is larger than the aperture of the upper opening of the reaction tank 2, the moving speed of the mixed liquor is gradually reduced, meanwhile, the liquid level of the mixed liquor slowly rises in the static settling tank 4, the mixed liquor can be settled in a stable state, and the rest CaSO4The particles are settled back to the reaction box 2 through the steady flow settling box 3 due to gravity, and supernatant of the mixed liquid in the static settling box 4 is discharged out of the homogeneous phase flow bed reactor 1 along a clear liquid port 12 on a clear liquid groove 11. Most of the CaSO in the reaction chamber 24The precipitated particles are discharged from a slag discharge port 16 of the reaction box 2, and a small amount of CaSO4The particles may remain in the reaction chamber 2 as seeds for subsequent reactions.
Referring to fig. 7, 8 and 9, there is shown a schematic diagram of a third embodiment of a homogeneousphase flow bed reactor configuration of the present invention. The device comprises a cylindrical reaction box 2, a polygonal steady flow settling box 3 arranged above the reaction box 2, and a cylindrical static settling box 4 which is arranged above the steady flow settling box 3 and has the caliber of the lower part larger than the caliber of an opening at the upper part of the reaction box 2; the upper part of the reaction box 2 is provided with an opening and is communicated with the steady flow settling box 3, the side wall of the reaction box 2 is provided with a raw material liquid inlet 14, a reaction liquid inlet 8, a flushing port 9, a clean discharging port 10 and a slag discharging port 16, a sampling port 13 is also arranged on the side wall of the reaction box 2 close to the upper opening, four stirrers 5 are uniformly distributed in the side wall of the reaction box 2, the central shafts of the stirrers 5 are inclined at a certain angle, the flushing port 9 is arranged above the stirrer 51, and the clean discharging port 10 is arranged below the stirrer 52; the steady flow settling tank 3 is a cavity with openings at the upper and lower parts, the lower opening of the steady flow settling tank is connected with the upper opening of the reaction tank 2 so as to be communicated with the reaction tank 2, the upper opening of the steady flow settling tank is connected and communicated with the static settling tank 3, the steady flow settling tank 3 is provided with a plurality of inverted frustum-shaped check rings 6 which are coaxially arranged at the interval of 300mm, the innermost inverted frustum-shaped check ring 6 is also provided with an inverted funnel-shaped bubble cap 7, the interval between the bottom cover edge of the bubble cap 7 and the innermost inverted frustum-shaped check ring 6 is 300mm, the top of the inverted funnel-shaped bubble cap 7 is also provided with a circulating pipe 8, one end of the circulating pipe 8 is communicated with the inverted funnel-shaped bubble cap 7, and the other end of the circulating pipe extends out of the outer wall of the; the lower opening of the static settling tank 4 is connected with the upper opening of the steady flow settling tank 3 so as to be communicated with the steady flow settling tank 3, the upper part of the static settling tank 4 is also provided with a clear liquid groove 11, the clear liquid groove 11 is provided with a clear liquid port 12, the upper part of the static settling tank 4 is also provided with an overflow groove 17, and the overflow groove 17 is provided with an overflow port 15.
The raw material liquid enters the reaction box 2 from the raw material liquid inlet 14 of the reaction box 2 and the reaction liquid enters the reaction box 2 from the reaction liquid inlet 8, the four stirrers 5 stir violently at the speed of 300 revolutions per minute, and the raw material liquid and the reaction liquid are rapidly reduced at the raw material liquid inlet 14 and the reaction liquid enterThe concentration near the opening 8 enables the raw material liquid and the reaction liquid to be quickly and uniformly mixed to form a mixed liquid, and CaSO is generated by reaction4Particles; in the reaction process, sampling from a sampling port 13 on the side wall of the reaction box 2 to detect and track the reaction progress; under the continuous stirring of the stirrer 5, the mixed liquid in the reaction box 2 stably and continuously enters the steady flow settling box 3 along with the gradual increase of the added raw material liquid and the added reaction liquid.
When the mixed liquid enters the steady flow settling tank 3, the CaSO in the mixed liquid4The particles are blocked by the retainer ring 6 and the bubble cap 7, the ascending speed of the particles is slowed, and most of CaSO4The particles are blocked to slide back into the reaction box 2, the mixed liquid blocked by the bubble cap 7 is uniformly distributed back to the peripheryof the reaction box 2 along the surface of the retainer ring 6, the dispersion of the mixed liquid is facilitated, the reaction is facilitated to be continued, the mixed liquid entering the bubble cap 7 quantitatively discharges the mixed liquid through the circulating port 10 arranged at the top of the mixed liquid, and the mixed liquid enters the reaction box 2 from the raw material liquid inlet 8 to continue to react, so that the reaction speed is slowed down, and the CaSO is enabled to be4The particles continue to grow until they become large-grained precipitate particles.
The mixed liquid after being blocked by a retainer ring 6 and a bubble cap 7 in the steady flow settling tank 3 contains CaSO4The number of particles is greatly reduced, the movement speed of the mixed liquor is slowed down, and the mixed liquor in the steady flow settling tank 3 continues to stably and continuously enter the static settling tank 4 along with the increase of substances in the reactor 1; because the aperture of the lower opening of the static settling tank 4 is larger than the aperture of the upper opening of the reaction tank 2, the movement speed of the mixed liquor is gradually reduced, meanwhile, the liquid level of the mixed liquor slowly rises in the static settling tank 4, the mixed liquor can be settled in a stable state, and the rest CaSO4The particles are settled back to the reaction box 2 through the steady flow settling box 3 due to gravity, supernatant of the mixed liquid in the static settling box 4 is discharged out of the homogeneous phase flow bed reactor 1 along a clear liquid port 12 on a clear liquid groove 11, and when the clear liquid amount is large, the supernatant is discharged out of the homogeneous phase flow bed reactor 1 through an overflow port 15 along an overflow groove 17. Most of the CaSO in the reaction chamber 24The particles are discharged from a slag discharge port 16 of the reaction box 2, and a small amountof CaSO4The particles can be left in the reaction chamber 2As a seed for the subsequent reaction.
When the reaction box 2 is cleaned, clean water is pumped from a washing port 9 on the side wall of the reaction box 2, and sewage is discharged from a clean discharge port 10 on the side wall of the reaction box 2.
Referring to fig. 10, 11 and 12, there is shown a schematic diagram of a fourth embodiment of a homogeneous phase flow bed reactor configuration of the present invention. The device comprises a square reaction box 2, a square steady flow settling box 3 arranged above the reaction box 2, and a square static settling box 4 arranged above the steady flow settling box 3, wherein the caliber of the lower part of the square static settling box is larger than that of an opening at the upper part of the reaction box 2; the upper part of the reaction box 2 is opened and is connected and communicated with the steady flow settling box 3, the side wall of the reaction box 2 is provided with a raw material liquid inlet 14, a reaction liquid inlet 8 and a slag discharge port 16, four stirrers 5 are uniformly distributed in the side wall of the reaction box 2, and the central shafts of the stirrers 5 are inclined at a certain angle; the steady flow settling tank 3 is a cavity with openings at the upper and lower parts, the opening at the lower part of the steady flow settling tank is connected with the opening at the upper part of the reaction tank 2 so as to be communicated with the reaction tank 2, the opening at the upper part of the steady flow settling tank is connected and communicated with the static settling tank 4, and the steady flow settling tank 3 is provided with a plurality of square check rings 6 which are arranged in the same direction at intervals of 250 mm; the lower opening of the static settling tank 4 is connected with the upper opening of the steady flow settling tank 3 so as to be communicated withthe steady flow settling tank 3, the upper part of the static settling tank 4 is also provided with a clear liquid groove 11, and the clear liquid groove 11 is provided with a clear liquid opening 12.
The raw material liquid enters the reaction box 2 from the raw material liquid inlet 14 of the reaction box 2 and the reaction liquid enters the reaction box 2 from the reaction liquid inlet 8, the four stirrers 5 stir violently at the speed of 300 revolutions per minute, the concentration of the raw material liquid and the reaction liquid near the raw material liquid inlet 14 and the reaction liquid inlet 8 is reduced rapidly, the raw material liquid and the reaction liquid are mixed uniformly rapidly to form a mixed liquid, and CaSO is generated through reaction4Particles; under the continuous stirring of the stirrer 5, the mixed liquid in the reaction box 2 stably and continuously enters the steady flow settling box 3 along with the gradual increase of the added raw material liquid and the added reaction liquid.
When the mixed liquid enters the steady flow settling tank 3, the CaSO in the mixed liquid4The particles are slowed down by the retaining ring 6, the rising speed of the particles is slowed down, and most of CaSO4The particles are prevented from sliding back into the reaction chamber 2, and the reaction is continued, so that CaSO4The particles continue to grow until they become large-grained precipitate particles.
The mixed liquid after being blocked by a retaining ring 6 in the steady flow settling tank 3 contains CaSO4The number of particles is greatly reduced, the movement speed of the mixed liquor is slowed down, and the mixed liquor in the steady flow settling tank 3 continues to stably and continuously enter the static settling tank 4 along with the increase of substances in the reactor 1; because the mixed liquor in the static settling tank 4is not stirred by external force any more, the moving speed of the mixed liquor is gradually reduced, meanwhile, because the caliber of the lower opening of the static settling tank 4 is larger than that of the upper opening of the reaction tank 2, the liquid level of the mixed liquor slowly rises in the static settling tank 4, the mixed liquor can be settled in a stable state, and the rest CaSO4The particles are settled back to the reaction box 2 through the steady flow settling box 3 due to gravity, and supernatant of the mixed liquid in the static settling box 4 is discharged out of the homogeneous phase flow bed reactor 1 from a clear liquid port 12 along a clear liquid tank 11. Most of the CaSO in the reaction chamber 24The particles are discharged from a slag discharge port 16 of the reaction box 2, and a small amount of CaSO4The particles may remain in the reaction chamber 2 as seeds for subsequent reactions.
From the above, the homogeneous phase flow bed reactor of the invention can effectively remove sulfate radicals accumulated in caustic soda production and prevent CaSO4Forming fine particles to form scale, and balancing the reaction at a certain temperature to obtain SO4 2-The ions are maximally precipitated, and the required molar concentration ratio of calcium ions can be reduced to Ca by using the homogeneous phase flow bed reactor2+∶SO4 2-＞1.5∶1。
The above-described embodiments are several implementations of the present invention, but the scope of the present invention is not limited to the specific descriptions in the above-described embodiments, and any modifications to the above-described embodiments according to the present invention, such as but not limited to the case 2, which may also have a prism shape, etc., are within the scope of the present invention.
Claims (14)
1. A homogeneous phase flow bed reactor, including a reaction box, the sidewall of the said reaction box has raw materials liquid inlet, reaction liquid inlet and slag hole, characterized by that, the said homogeneous phase flow bed reactor also includes a steady flow settling tank set up above the said reaction box, and a static settling tank set up above the said steady flow settling tank; the upper part of the reaction box is opened and is connected and communicated with the steady flow settling box, and two or more than two stirrers are uniformly distributed in the side wall of the reaction box; the steady flow settling tank is a cavity with openings at the upper part and the lower part, the opening at the lower part of the steady flow settling tank is connected with the opening at the upper part of the reaction tank so as to be communicated with the reaction tank, the opening at the upper part of the steady flow settling tank is connected and communicated with the static settling tank, and the steady flow settling tank comprises a plurality of layers of check rings which are arranged at intervals; the lower opening of the static settling tank is connected with the upper opening of the steady flow settling tank so as to be communicated with the steady flow settling tank, the caliber of the lower opening of the static settling tank is larger than that of the upper opening of the reaction tank, and the static settling tank is provided with a clear liquid port.
2. A homogeneous flow bed reactor according to claim 1, wherein said baffle is a coaxial spaced baffle.
3. A homogeneous flow bed reactor according to claim 1, wherein said baffle ring is of an inverted truncated cone shape.
4. Thehomogeneous flow bed reactor according to claim 1, wherein the retaining ring is in the shape of an inverted frustum of a pyramid.
5. A homogeneous flow bed reactor according to claim 1, wherein said reaction liquid inlet is disposed above said agitator.
6. The homogeneous phase flow bed reactor according to claim 1, wherein the side wall of the reaction chamber is further provided with a flushing port and a purging port.
7. The homogeneous phase flow bed reactor according to claim 1, wherein a sampling port is further provided on the sidewall of said reaction chamber near the upper opening.
8. The homogeneous flow bed reactor according to claim 1, wherein the agitator is inserted diagonally into the side wall of the reaction tank, and the agitator is an agitator rotating at a speed of more than 250 rpm.
9. The homogeneous phase flow reactor according to claim 1, wherein an inverted funnel-shaped bubble cap is coaxially arranged in the retaining ring at the innermost ring in the steady flow settling tank, a circulating pipe is arranged at the top of the inverted funnel-shaped bubble cap, one end of the circulating pipe is communicated with the inverted funnel-shaped bubble cap, and the other end of the circulating pipe is connected with the reaction liquid inlet on the reaction tank.
10. The homogeneous flow bed reactor according to claim 1, wherein the distance between the retaining rings is 150-300 mm.
11. The homogeneous flow bed reactor according to claim 1, wherein the distance between the bottom cap edge of the inverted funnel-shaped bubble cap and the innermost collar is 150-300 mm.
12. The homogeneous flow bed reactor according to claim 1, wherein a clear liquid tank is further provided at the upper part of the static settling tank, and the clear liquid tank is communicated with a clear liquid port of the static settling tank.
13. The homogeneous phase flow bed reactor according to claim 12, wherein said static settling tank further comprises an overflow tank disposed at an upper portion thereof, said overflow tank being provided with an overflow port.
14. The homogeneous flow bed reactor according to claim 13, wherein said overflow launder is provided at an upper portion of said clear liquid launder.
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| FR2305393A1 (en) * | 1975-03-28 | 1976-10-22 | Rhone Poulenc Ind | NEW PROCESS FOR OBTAINING CAUSTIC SODA FROM A CHLORUROSODIUM LESSIVE, CONTAINING SULPHATE IONS, PROVIDED BY AN ELECTROLYSIS CELL |
| US4565612A (en) * | 1984-12-10 | 1986-01-21 | The Dow Chemical Company | Process for reducing sulphate ion concentration in aqueous sodium hydroxide solutions |
| CN1019095B (en) * | 1989-06-17 | 1992-11-18 | 自贡市张家坝制盐化工厂 | Method for removing ions of calcium and sulfuric acid radical from common salt brine and bittern |
| CN1169397A (en) * | 1996-06-26 | 1998-01-07 | 李运生 | Ternary brine denitration liquid |
| CN1193934C (en) * | 2002-09-20 | 2005-03-23 | 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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2005
- 2005-04-07 CN CNB2005100249617A patent/CN100358623C/en active Active
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