CN108101091B - Method and device for producing calcium carbonate by dynamic carbonization method - Google Patents
Method and device for producing calcium carbonate by dynamic carbonization method Download PDFInfo
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- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 title claims abstract description 118
- 238000003763 carbonization Methods 0.000 title claims abstract description 81
- 229910000019 calcium carbonate Inorganic materials 0.000 title claims abstract description 57
- 238000000034 method Methods 0.000 title claims abstract description 57
- 238000006243 chemical reaction Methods 0.000 claims abstract description 75
- 239000002002 slurry Substances 0.000 claims abstract description 57
- 239000011575 calcium Substances 0.000 claims abstract description 29
- 238000005507 spraying Methods 0.000 claims abstract description 27
- 238000004519 manufacturing process Methods 0.000 claims abstract description 19
- 238000010992 reflux Methods 0.000 claims abstract description 15
- 238000002156 mixing Methods 0.000 claims abstract description 10
- 239000012066 reaction slurry Substances 0.000 claims abstract description 8
- 238000012544 monitoring process Methods 0.000 claims abstract description 5
- 238000005086 pumping Methods 0.000 claims abstract description 5
- 239000007788 liquid Substances 0.000 claims description 31
- 238000009826 distribution Methods 0.000 claims description 6
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 38
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract description 18
- 239000002245 particle Substances 0.000 abstract description 17
- 239000001569 carbon dioxide Substances 0.000 abstract description 9
- 230000008901 benefit Effects 0.000 abstract description 6
- 239000000920 calcium hydroxide Substances 0.000 description 20
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 20
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 17
- 239000013078 crystal Substances 0.000 description 14
- 210000004940 nucleus Anatomy 0.000 description 9
- 230000008569 process Effects 0.000 description 9
- 239000012071 phase Substances 0.000 description 8
- 230000002035 prolonged effect Effects 0.000 description 8
- 230000035484 reaction time Effects 0.000 description 8
- 239000007791 liquid phase Substances 0.000 description 7
- 230000000694 effects Effects 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 4
- 230000005611 electricity Effects 0.000 description 3
- 230000002349 favourable effect Effects 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- 230000003068 static effect Effects 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 2
- 239000000292 calcium oxide Substances 0.000 description 2
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 238000010008 shearing Methods 0.000 description 2
- 238000009423 ventilation Methods 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 238000010000 carbonizing Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 239000000839 emulsion Substances 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000001879 gelation Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000004381 surface treatment Methods 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F11/00—Compounds of calcium, strontium, or barium
- C01F11/18—Carbonates
- C01F11/181—Preparation of calcium carbonate by carbonation of aqueous solutions and characterised by control of the carbonation conditions
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2004/00—Particle morphology
- C01P2004/60—Particles characterised by their size
- C01P2004/61—Micrometer sized, i.e. from 1-100 micrometer
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Inorganic Chemistry (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Abstract
The invention relates to the technical field of calcium carbonate production, and particularly discloses a method and a device for producing calcium carbonate by a dynamic carbonization method. The method comprises the following steps: suspending and limiting a dynamic reactor with a reaction cavity and a downward opening in the reaction tankThe reaction tank is added with blended Ca (OH)2A slurry, and submerging an opening of the dynamic reactor; pumping the Ca (OH) in the reaction tank by a reflux pump2Spraying and refluxing the slurry into a reaction cavity of the dynamic reactor; simultaneously, introducing CO into the reaction cavity2Mixing the gas; and monitoring the pH value of the reaction slurry in the reaction tank, and stopping slurry backflow when the pH value is 7-8 to obtain a crude calcium carbonate product. The method and the device for producing calcium carbonate by the dynamic carbonization method provided by the invention have the advantages that the carbonization speed is improved by 60%, the carbonization time is shortened by 37.5%, the particle size of the generated calcium carbonate is 2-4 microns, and the utilization rate of carbon dioxide is improved to 69% from the original 50%.
Description
Technical Field
The invention relates to the technical field of calcium carbonate production, in particular to a method and a device for producing calcium carbonate by a dynamic carbonization method.
Background
At present, the main method for producing light calcium carbonate at home and abroad is a calcium hydroxide carbonization method. The method is to calcine selected limestone to obtain calcium oxide and kiln gas. Digesting calcium oxide, crushing the generated suspended calcium hydroxide under the action of high shear force, and performing multi-stage hydrocyclone separation to remove particles and impurities to obtain a refined calcium hydroxide suspension with a certain concentration; then introducing carbon dioxide gas, adding a proper crystal form control agent, and carbonizing to the end point to obtain crystal form calcium carbonate slurry; and finally, carrying out dehydration, drying and surface treatment to obtain the superfine calcium carbonate product.
The carbonization method includes a static carbonization method and a dynamic carbonization method. The processes adopted at home and abroad comprise an intermittent bubbling type carbonization method, a stirring type carbonization method and a spraying continuous carbonization method, which are all static carbonization methods; the supergravity carbonization method is dynamic carbonization. The static carbonization mode mainly has the defects of long carbonization time, high power consumption, low carbon dioxide utilization rate, uncontrollable process, large product granularity, wide distribution range and the like. The hypergravity carbonization method is a dynamic method, so that the transfer process and the micro mixing process of the reactor are fundamentally strengthened. But has the defects of complex operation, too large power consumption and the like.
Disclosure of Invention
Aiming at the problems of large consumption, low utilization rate of carbon dioxide and the like of the existing dynamic method, the invention provides a method for producing calcium carbonate by a dynamic carbonization method.
The invention also provides a device for producing calcium carbonate by using the dynamic carbonization method.
In order to achieve the purpose of the invention, the embodiment of the invention adopts the following technical scheme:
a method for producing calcium carbonate by dynamic carbonization, the method comprising at least the steps of:
suspending a dynamic reactor with a reaction cavity and a downward opening in a reaction tank, adding Ca (OH) into the reaction tank2A slurry, and submerging an opening of the dynamic reactor;
pumping the Ca (OH) in the reaction tank by a reflux pump2Spraying and refluxing the slurry into a reaction cavity of the dynamic reactor;
simultaneously, introducing CO into the reaction cavity2Mixing the gas;
and step three, monitoring the pH value of the reaction slurry in the reaction tank, and stopping slurry backflow when the pH value is 7-8 to obtain a crude calcium carbonate product.
The method for producing calcium carbonate by the dynamic carbonization method provided by the invention has the following advantages:
reflux pump Ca (OH)2The slurry is added in the reaction tank in a circulating spraying manner, the calcium hydroxide slurry is a dispersed phase, and the gas is a continuous phase, so that the gas-liquid contact surface is greatly increased, the residence time of the fog drops in the dynamic reactor is prolonged, the gas-liquid contact time is prolonged, crystal nuclei are quickly formed, the carbonization reaction is facilitated, and the carbonization time is saved;
according to the method for producing calcium carbonate by using the dynamic carbonization method, the carbonization speed is expressed by the amount of the produced calcium carbonate in unit time, the carbonization speed in the prior art is 1.5t/h, and the carbonization speed in the prior art is 2.4 t/h. The carbonization speed is improved by 60 percent. The carbonization time per ton is shortened by 0.25h and 37.5 percent. The grain size of the generated superfine calcium carbonate is 2-4 microns and less than 5 microns, and the whiteness reaches 94.8. The emission of carbon dioxide is reduced, and the utilization rate of the carbon dioxide is improved to 69 percent from the original 50 percent.
Correspondingly, the invention also provides a device for producing calcium carbonate by using a dynamic carbonization method, which comprises a reaction tank and also comprises:
the dynamic reactor is suspended and limited in the reaction tank, the bottom end of the dynamic reactor is provided with an opening, and the dynamic reactor is provided with an umbrella-shaped gas distributor;
CO2proportioner for blending CO2The volume content of the gas is communicated with the upper end of the dynamic reactor through a pipeline;
and the liquid inlet end of the slurry return pipe is communicated with a return port at the bottom of the reaction tank, and the liquid outlet end of the slurry return pipe is communicated with the upper end of the dynamic reactor through a return pump.
Compared with the prior art, the device for producing calcium carbonate by the dynamic carbonization method is simple, the slurry backflow pipe and the backflow pump are used for circularly adding the calcium hydroxide slurry, the calcium hydroxide slurry is a dispersed phase, the gas is a continuous phase, the gas-liquid contact surface is greatly increased, the residence time of fog drops in the dynamic reactor is prolonged, the gas-liquid contact time is prolonged, crystal nuclei are quickly formed, the carbonization reaction is facilitated, and the carbonization time is saved;
is arranged at the upper part of a dynamic reactor and is connected with CO2The proportioners are communicated and used for blending CO2The volume content of the gas is favorable for the reaction, and CO2The resistance of the reactor entering the device is smaller than that of the reactor entering the gas from the lower part, so that the power consumption is reduced, and the investment is greatly reduced; meanwhile, the upper part of the reactor is charged with air, so that a reaction path can be increased in the dynamic reactor, and the carbonization reaction time is saved;
umbrella-shaped gas distributor for distributing CO2The gas is uniformly dispersed without forming large bubbles, so that CO is generated2The gas and the calcium hydroxide in the reaction tank are carbonized again, the slurry backflow pipe enables the calcium hydroxide slurry to flow all the time and fully react, the final carbonization speed is improved by 60 percent, and CO is reduced2The utilization rate is improved by 20 percent, and the effects of reducing energy consumption and being simple to operate are finally achieved.
Drawings
In order to more clearly illustrate the technical solutions in the embodiments of the present invention, the drawings needed to be used in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art that other drawings can be obtained according to these drawings without creative efforts.
FIG. 1 is a schematic view of a dynamic carbonization reaction apparatus according to an embodiment of the present invention;
FIG. 2 is a schematic top view of an umbrella gas distributor according to an embodiment of the present invention.
Wherein: 11. CO 22A bottle; 12. an air pump; 13. a flow meter; 14. CO 22A proportioner; 21. a reaction tank; 22. a slurry return pipe; 23. a pH measuring device; 24. a spraying device; 25. a dynamic reactor; 26. An umbrella-shaped gas distributor; 27. distributing air holes; 28. saw teeth; 29. a reflux pump; 30. and (4) a discharge port.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is further described in detail with reference to the following embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
A method for producing calcium carbonate by dynamic carbonization, the method comprising at least the steps of:
suspending a dynamic reactor with a reaction cavity and a downward opening in a reaction tank, adding Ca (OH) into the reaction tank2A slurry, and submerging an opening of the dynamic reactor;
pumping the Ca (OH) in the reaction tank by a reflux pump2Spraying and refluxing the slurry into a reaction cavity of the dynamic reactor;
simultaneously, introducing CO into the reaction cavity2Mixing the gas;
and step three, monitoring the pH value of the reaction slurry in the reaction tank, and stopping slurry backflow when the pH value is 7-8 to obtain a crude calcium carbonate product.
The method for producing calcium carbonate by the dynamic carbonization method provided by the invention has the following advantages:
according to the method for producing calcium carbonate by using the dynamic carbonization method, the carbonization speed is expressed by the amount of the produced calcium carbonate in unit time, the carbonization speed in the prior art is 1.5t/h, and the carbonization speed in the prior art is 2.4 t/h. The carbonization speed is improved by 60 percent. The carbonization time per ton is shortened by 0.25h and 37.5 percent. The grain size of the generated superfine calcium carbonate is 2-4 microns and less than 5 microns, and the whiteness reaches 94.8. The emission of carbon dioxide is reduced, and the utilization rate of the carbon dioxide is improved to 69 percent from the original 50 percent.
Preferably, in step one, the Ca (OH)2The concentration of the slurry is 8-10 wt%, and the temperature is 40-50 ℃.
Ca(OH)2Influence of slurry concentration on calcium carbonate particle size: ca (OH)2At lower concentrations, the calcium carbonate particle size is smaller. When Ca (OH)2After the concentration exceeds 10 percent, the temperature of the system rises too fast due to heat release of carbonization, the carbonization process is more powerful than crystal growth, large crystals are generated, and the viscosity of the system is obviously increased, so that the gelation phenomenon is serious in the carbonization process, the movement of crystal nucleus particles is hindered, conditions are provided for the agglomeration of the particles, and the product particles are enlarged; further, Ca (OH)2The concentration is high, the particle collision in the reaction process is aggravated, and the stability of newly generated calcium carbonate crystals can be influenced, so that the calcium carbonate grains are larger.
Ca(OH)2Effect of slurry concentration on reaction time: with Ca (OH)2The carbonization reaction time increases with an increase in the concentration. Ca (OH)2When the concentration is lower, the consistency and the viscosity of the reaction system are smaller, the influence of the increase of the concentration on the fluid mechanical property is not large, and the increase amplitude of the reaction time is smaller. Ca (OH)2When the concentration exceeds a certain value, the viscosity of the emulsion is increased, the particles move slowly, the liquid film resistance of a solid-liquid interface is increased, and CO is generated2The dissolution and mass transfer become difficult, so that the carbonization time is prolonged. Increase Ca (OH)2The concentration is favorable for the reaction and the CO is increased2Absorption rate. When the concentration exceeds 10%, a gel phenomenon appears, and the gel phenomenon has great influence on the processes of mixing, heat transfer, gas-liquid-solid mass transfer and the like among system materials. Particle size of calcium carbonateThe carbonization time is prolonged. However, the concentration of calcium hydroxide cannot be too low, which causes the reduction of the production capacity of equipment, the increase of energy consumption, the increase of cost and the generation of more waste water, and the proper concentration of calcium hydroxide is about 8-10 percent in combination with the above results.
Preferably, in step one, the Ca (OH)2The flow rate of slurry spraying and refluxing is 35-40m3/h。
Ca(OH)2Influence of slurry spraying reflux flow on calcium carbonate particle size: with Ca (OH)2The increase of the slurry flow has less influence on the particle size, the carbonization time is shortened, and CO2The utilization rate is improved. CO 22High ventilation in Ca (OH)2At very low slurry flow rates, Ca (OH)2Limited rate of dissolution, CO2In excess. On the other hand, Ca (OH)2The slurry flow is small, the shearing force to gas is small, the diameter of bubbles entering the liquid phase is large, and mass transfer is not facilitated, so that Ca (OH)2CO when the slurry flow is small2The utilization rate is low. Because the carbonization reaction is intermittent operation, and the increase of the liquid flow rate means that the liquid circulation times in unit time are increased, the contact chance with gas is increased, the mass transfer surface area is increased, and CO is strengthened2The absorption of (2) is favorable for shortening the carbonization time. The shearing force is increased along with the increase of the liquid phase flow, the diameter of the bubbles is reduced, meanwhile, the increase of the liquid flow is equivalent to the increase of the flow velocity of a liquid nozzle, the liquid is favorably thinned into small liquid drops, and the particle size is reduced along with the increase of the flow. Therefore, the conditions of power and the like of production equipment are comprehensively considered.
Preferably, in step two, the mixed gas is air and CO2In which CO is2The volume content of the mixed gas is 25-35%, and the flow rate of the mixed gas is 40-50m3/min。
The change in the flow of the mixed gas has an effect on the reaction time and the particle size of the calcium carbonate: the flow of the mixed gas is increased to facilitate CO on a gas-liquid interface2The increase of equilibrium concentration increases the mass transfer rate from gas phase to liquid phase, strengthens the transfer process, and has large gas-liquid contact area and shortened reaction time. Since the carbonization reaction is carried out at the phase boundary, increaseThe gas flow can increase the gas-liquid contact area and accelerate the carbonization reaction. However, the gas flow is too large, the gas-liquid contact area is basically kept unchanged, and the gas escapes without being dispersed in the liquid phase and does not participate in the reaction. Even if the gas flow is continuously increased, the CO is not obviously improved2Gas-liquid mass transfer between liquid phase and liquid phase, reaction to make CO go up2The utilization rate is reduced and thus the reaction time is substantially unchanged. CO 22The increase of flow makes reaction rate accelerate, produces a large amount of crystal nucleuses in the twinkling of an eye in the liquid phase, makes the calcium carbonate supersaturation degree of generating increase, and the particle diameter reduces, and along with the going on of reaction, the crystal nucleus grows for the crystalline grain through constantly colliding with the crystal nucleus, and when the growth rate of crystal nucleus was greater than the growth rate of crystal nucleus, the particle that obtains was great.
Preferably, the open end of the dynamic reactor is provided with an umbrella-shaped gas distributor, and the periphery of the bottom edge of the dynamic reactor is provided with sawteeth. The umbrella-shaped gas distributor is immersed below the liquid level of the reaction slurry, and is provided with gas distribution holes with the aperture of 0.8-1.5cm and the interval of 1.5-2 cm.
Umbrella-shaped gas distributor for distributing CO2The gas is uniformly dispersed without forming large bubbles, so that CO is generated2The gas and the calcium hydroxide in the reaction tank are carbonized again, the slurry backflow pipe enables the calcium hydroxide slurry to flow all the time and fully react, the final carbonization speed is improved by 60 percent, and CO is reduced2The utilization rate is improved by 20 percent, and the effects of reducing energy consumption and being simple to operate are finally achieved.
Further, the embodiment of the present invention provides an apparatus for producing calcium carbonate by a dynamic carbonization method, including a reaction tank 21, further including:
the dynamic reactor 25 is suspended and limited in the reaction tank 21, the bottom end of the dynamic reactor 25 is provided with an opening, and an umbrella-shaped gas distributor 26 is arranged on the bottom end of the dynamic reactor 25;
CO2proportioner 14 for blending CO2The volume content of the gas and is communicated with the upper end of the dynamic reactor 26 through a pipeline;
and a slurry return pipe 22, wherein the liquid inlet end of the slurry return pipe is communicated with a return port at the bottom of the reaction tank 21, and the liquid outlet end of the slurry return pipe is communicated with the upper end of the dynamic reactor 25 through a return pump 29.
Compared with the prior art, the device for producing calcium carbonate by the dynamic carbonization method is simple, the calcium hydroxide slurry is circularly added through the slurry return pipe 22 and the return pump 29, the calcium hydroxide slurry is in a dispersed phase, and the gas is in a continuous phase, so that the gas-liquid contact surface is greatly increased, the residence time of fog drops in the dynamic reactor 25 is prolonged, the gas-liquid contact time is prolonged, crystal nuclei are quickly formed, the carbonization reaction is facilitated, and the carbonization time is saved;
is arranged at the upper part of a dynamic reactor 25 and is connected with CO2The proportioner 14 is communicated with CO2The resistance of the reactor entering the device is smaller than that of the reactor entering the gas from the lower part, so that the power consumption is reduced, and the investment is greatly reduced; meanwhile, the upper part of the reactor is charged with air, so that a reaction path can be increased in the dynamic reactor, and the carbonization reaction time is saved;
Preferably, the outlet end of the slurry return pipe 22 is provided with a spraying device 24. The spraying device 24 is 3 spraying heads connected through a three-way pipe, and spraying holes with the aperture of 1-2cm are formed in the spraying heads.
The spray device 24 forms the calcium hydroxide slurry into high-speed jet flow and CO2Full contact, increase of CO2The utilization ratio of (2). The spray holes on the spray header are too small in aperture, easy to block and too large, and cannot achieve the technical effect.
Preferably, the CO is2The proportioning device 14 is provided with an air inlet and CO2Gas inlet and CO2A mixed gas outlet, the air inlet is communicated with the air outlet of the air pump 12, and the CO is2Gas inlet and CO2Bottle 11 is communicated with the CO2The mixed gas outlet is communicated with the upper end of the dynamic reactor 25 through a pipeline.
By CO in the course of the reaction2Proportioning device 14 for proportioning CO2The mixed gas with proper concentration is suitable for preparing calcium carbonate by a dynamic reaction method.
Preferably, a pH measuring device 23 is disposed on a side wall of the reaction tank 21.
Preferably, the bottom end of the reaction tank 21 is provided with a discharge hole 30.
The following examples are provided to better illustrate the embodiments of the present invention.
Example 1
The embodiment of the invention provides a device for producing calcium carbonate by a dynamic carbonization method, which comprises a reaction tank 21 and also comprises the following components by referring to the attached figures 1 and 2: the dynamic reactor 25 is suspended and limited in the reaction tank 21, the bottom end of the dynamic reactor 25 is provided with an opening, and an umbrella-shaped gas distributor 26 is arranged on the bottom end of the dynamic reactor 25;
CO2proportioner 14 for blending CO2The volume content of the gas and is communicated with the upper end of the dynamic reactor 26 through a pipeline;
a slurry return pipe 22, the liquid inlet end of which is communicated with the return port at the bottom of the reaction tank 21, and the liquid outlet end of which is communicated with the upper end of the dynamic reactor 25 through a return pump 29;
and the pH measuring device 23 is arranged on the side wall of the reaction tank 21.
The outlet end of the slurry return pipe 22 is provided with a spraying device 24. The spraying device 24 is 3 spraying heads connected through a three-way pipe, and spraying holes with the aperture of 1-2cm are formed in the spraying heads.
CO as described above2The proportioning device 14 is respectively connected with the air outlet of the air pump 14 and CO2Bottle 11 is communicated with each other, and CO2Proportioning device 14, CO2The bottle 11 and the air pump 12 are also provided with a flow meter 13 and a valve.
The umbrella-shaped gas distributor 26 is immersed below the liquid level of the reaction slurry, and the circumference of the bottom edge is provided with saw teeth 28. The umbrella-shaped gas distributor 26 is provided with gas distribution holes, the aperture of the gas distribution holes 27 is 0.8-1.5cm, and the distance is 1.5-2 cm.
The bottom end of the reaction tank 21 is provided with a discharge hole 30.
The embodiment of the invention also provides a method for producing calcium carbonate by a dynamic carbonization method, and the device for producing calcium carbonate by the dynamic carbonization method comprises the following steps:
suspending a dynamic reactor with a reaction cavity and a downward opening in a reaction tank, adding Ca (OH) into the reaction tank2Slurry and submerging the opening of the dynamic reactor, wherein Ca (OH)2The temperature of the slurry was 45 ℃ Ca (OH)2The slurry concentration was 8 wt%;
pumping the Ca (OH) in the reaction tank by a reflux pump2Spraying the slurry into the reaction cavity of the dynamic reactor for backflow, wherein Ca (OH)2The flow rate of slurry spraying and refluxing is 40m3/h；
Simultaneously, introducing CO into a reaction cavity of the dynamic reactor2Mixed gas with a ventilation of 45m3Min, CO in the mixed gas2The volume content of (A) is 30%;
and step three, monitoring the pH value of the reaction slurry in the reaction tank, and stopping slurry backflow when the pH value is 7-8 to obtain a crude calcium carbonate product.
The calcium carbonate prepared by the method for producing calcium carbonate by dynamic carbonization in the example was examined. The average grain diameter of the product is 2-4um, the grain diameter of the product is uniform, the distribution is narrow and the quality is stable through the analysis of a laser particle analyzer. The content and the like all reach the industrial grade standard and meet the national product standard.
Compared with the prior art: theoretically, pure CO is consumed for every 1t of calcium carbonate produced20.44t。
In the prior art: CO in batch carbonization process2The utilization rate of the catalyst is only 50 percent, and pure CO is consumed for producing 1t of calcium carbonate20.88t, kiln gas CO2The content is 30 percent, and the kiln gas is 1960m3CO emitted in the carbonization process2The number of (2) is 0.44 t.
The method for producing calcium carbonate by using the dynamic carbonization method provided in the embodiment is CO2The utilization rate of the calcium carbonate can reach 69 percent, and pure CO is consumed for actually producing 1t of calcium carbonate20.64t, the carbon dioxide content of the kiln gas is 30 percent, and the actual required kiln gas is 1423m3. Then, CO discharged from the carbonization process2The mass of the catalyst is only 0.20t, and CO is emitted less than one year24363200m3Energy conservation and environmental protection, and good social benefit.
The method and the device for producing the calcium carbonate by adopting the dynamic carbonization method shorten the carbonization time, save electricity of 11.4 degrees per ton, save electricity of 492480 degrees per year, reduce the ton cost by 8.89 yuan and save the cost by 38 ten thousand yuan per year according to 0.78 yuan per ton of electricity, and have considerable benefits.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents or improvements made within the spirit and principle of the present invention should be included in the scope of the present invention.
Claims (8)
1. A method for producing calcium carbonate by a dynamic carbonization method is characterized by comprising the following steps: the method comprises at least the following steps:
suspending a dynamic reactor with a reaction cavity and a downward opening in a reaction tank, adding Ca (OH) into the reaction tank2Slurry and submerging the opening of the dynamic reactor, the Ca (OH)2The slurry concentration is 8-10 wt%, the temperature is 40-50 deg.C, the Ca (OH) is2The flow rate of slurry spraying and refluxing is 35-40m3/h；
Pumping the Ca (OH) in the reaction tank by a reflux pump2Spraying and refluxing the slurry into a reaction cavity of the dynamic reactor;
simultaneously, introducing CO into the reaction cavity2Mixed gas of air and CO2In which CO is2The volume content of the mixed gas is 25-35%, and the flow rate of the mixed gas is 40-50m3/min；
And step three, monitoring the pH value of the reaction slurry in the reaction tank, and stopping slurry backflow when the pH value is 7-8 to obtain a crude calcium carbonate product.
2. The method for producing calcium carbonate according to claim 1, wherein: the open end of the dynamic reactor is provided with an umbrella-shaped gas distributor, and the periphery of the bottom edge of the dynamic reactor is provided with sawteeth.
3. The method for producing calcium carbonate according to claim 2, wherein: the umbrella-shaped gas distributor is immersed below the liquid level of the reaction slurry, and is provided with gas distribution holes with the aperture of 0.8-1.5cm and the interval of 1.5-2 cm.
4. The utility model provides a device of dynamic carbonization method production calcium carbonate, includes the retort, its characterized in that still includes:
the dynamic reactor is suspended and limited in the reaction tank, the bottom end of the dynamic reactor is provided with an opening, and the dynamic reactor is provided with an umbrella-shaped gas distributor;
CO2proportioner for blending CO2The volume content of the gas is communicated with the upper end of the dynamic reactor through a pipeline;
and the liquid inlet end of the slurry return pipe is communicated with a return port at the bottom of the reaction tank, and the liquid outlet end of the slurry return pipe is communicated with the upper end of the dynamic reactor through a return pump.
5. The apparatus for producing calcium carbonate by dynamic carbonization according to claim 4, wherein: and a spraying device is arranged at the liquid outlet end of the slurry return pipe.
6. The apparatus for producing calcium carbonate by dynamic carbonization according to claim 5, wherein: the spraying device is provided with 3 spraying heads connected through a three-way pipe, and the spraying heads are provided with spraying holes with the aperture of 1-2 cm.
7. The apparatus for producing calcium carbonate by dynamic carbonization according to claim 4, wherein: the CO is2The proportioning device is provided with an air inlet and CO2Gas inlet and CO2A mixed gas outlet, the air inlet and the outlet of the air pumpThe tuyere is communicated with the CO2Gas inlet and CO2Bottle to bottle, the CO2The mixed gas outlet is communicated with the upper end of the dynamic reactor through a pipeline.
8. The apparatus for producing calcium carbonate by dynamic carbonization according to claim 4, wherein: and a pH measuring device is arranged on the side wall of the reaction tank.
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| CN113173685B (en) * | 2021-05-06 | 2023-04-14 | 徐州天瑞邦公共卫生防控研究院有限公司 | Carbonization box for material recovery based on salt mud innocent treatment |
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| CN103738993B (en) * | 2013-12-04 | 2015-11-04 | 芜湖卓越纳米新材料有限公司 | A kind of carbonization reactor of energy-saving nano-calcium carbonate and preparation method |
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