CN108101091A - A kind of method and apparatus of dynamic carbonizatin method production calcium carbonate - Google Patents
A kind of method and apparatus of dynamic carbonizatin method production calcium carbonate Download PDFInfo
- Publication number
- CN108101091A CN108101091A CN201711487518.2A CN201711487518A CN108101091A CN 108101091 A CN108101091 A CN 108101091A CN 201711487518 A CN201711487518 A CN 201711487518A CN 108101091 A CN108101091 A CN 108101091A
- Authority
- CN
- China
- Prior art keywords
- dynamic
- calcium carbonate
- retort
- response device
- slurry
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 title claims abstract description 119
- 238000000034 method Methods 0.000 title claims abstract description 80
- 229910000019 calcium carbonate Inorganic materials 0.000 title claims abstract description 59
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 38
- 239000002002 slurry Substances 0.000 claims abstract description 52
- 230000004044 response Effects 0.000 claims abstract description 44
- 238000006243 chemical reaction Methods 0.000 claims abstract description 40
- 239000011575 calcium Substances 0.000 claims abstract description 26
- 238000010992 reflux Methods 0.000 claims abstract description 26
- 239000000725 suspension Substances 0.000 claims abstract description 11
- 239000012043 crude product Substances 0.000 claims abstract description 5
- 239000007921 spray Substances 0.000 claims description 27
- 239000000920 calcium hydroxide Substances 0.000 claims description 23
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 23
- 239000007788 liquid Substances 0.000 claims description 18
- 230000008676 import Effects 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 4
- 238000012544 monitoring process Methods 0.000 claims description 4
- -1 retort Chemical compound 0.000 claims description 3
- 229910052791 calcium Inorganic materials 0.000 claims description 2
- 229910052799 carbon Inorganic materials 0.000 claims description 2
- 238000009826 distribution Methods 0.000 claims description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims 1
- 239000004744 fabric Substances 0.000 claims 1
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 62
- 238000003763 carbonization Methods 0.000 abstract description 34
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract description 18
- 239000001569 carbon dioxide Substances 0.000 abstract description 6
- 239000007789 gas Substances 0.000 description 56
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical group [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 15
- 238000005255 carburizing Methods 0.000 description 12
- 239000003153 chemical reaction reagent Substances 0.000 description 12
- 239000000047 product Substances 0.000 description 8
- 239000002245 particle Substances 0.000 description 7
- 239000012071 phase Substances 0.000 description 7
- 239000007791 liquid phase Substances 0.000 description 6
- 230000008901 benefit Effects 0.000 description 5
- 239000013078 crystal Substances 0.000 description 5
- 230000005611 electricity Effects 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 230000035484 reaction time Effects 0.000 description 5
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 4
- 239000000292 calcium oxide Substances 0.000 description 4
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 230000009467 reduction Effects 0.000 description 4
- 239000012530 fluid Substances 0.000 description 3
- 239000000843 powder Substances 0.000 description 3
- 230000003068 static effect Effects 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 230000001351 cycling effect Effects 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 238000010008 shearing Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 108010010803 Gelatin Proteins 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000004090 dissolution 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
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000686 essence Substances 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000000499 gel Substances 0.000 description 1
- 239000008273 gelatin Substances 0.000 description 1
- 229920000159 gelatin Polymers 0.000 description 1
- 235000019322 gelatine Nutrition 0.000 description 1
- 235000011852 gelatine desserts Nutrition 0.000 description 1
- 230000006872 improvement Effects 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
- 229940088417 precipitated calcium carbonate Drugs 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000004381 surface treatment Methods 0.000 description 1
- 238000002834 transmittance Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- 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
Landscapes
- 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 present invention relates to calcium carbonate production technical fields, specifically disclose a kind of method and apparatus of dynamic carbonizatin method production calcium carbonate.The method, which uses, to be included：Suspension /V one is equipped with reaction chamber, downward opening dynamic response device in retort, and the Ca (OH) of allotment is added in the retort2Slurry, and submerge the opening of the dynamic response device；The Ca (OH) in the retort is extracted by reflux pump2Slurry, and reflux is sprayed into the reaction chamber of the dynamic response device；Meanwhile it is passed through into the reaction chamber containing CO2Mixed gas；The pH value of the reaction paste in the retort is monitored, when pH value is 78, stops backflow of slurry, calcium carbonate crude product is made.The method and apparatus of dynamic carbonizatin method production calcium carbonate provided by the invention, carbonization speed improve 60%, and carbonization time shortens 37.5%, and 24 microns of generation calcium carbonate grain size, utilization rate of carbon dioxide is increased to 69% by original 50%.
Description
Technical field
The present invention relates to calcium carbonate production technical field more particularly to a kind of dynamic carbonizatin method production calcium carbonate method and
Device.
Background technology
The main method of production precipitated calcium carbonate is calcium hydroxide carbonizatin method both at home and abroad at present.This method is will be selected
Limestone calcination obtains calcium oxide and kiln gas.Calcium oxide is digested, and by the suspension calcium hydroxide of generation in high shear
Lower crushing, multistage rotary filter press remove degranulation and impurity, obtain certain density refined calcium hydroxide suspension；Then pass to two
Carbon oxide gas, add in appropriate chemical additives, and carbonization to terminal, obtains the calcium carbonate serosity of crystal form；Finally using de-
Water, drying, surface treatment obtain calcium carbonate superfine powder product.
The static carbonizatin method of carbonizatin method point and dynamic carbonizatin method.The technique used both at home and abroad has interval bubble type carbonizatin method, stirs
Formula carbonizatin method, spraying continuous carbonization method are mixed, is static carbonizatin method；High-gravity carbonation method is carbonized for dynamic.Static carbonization mode
It is primarily present long carbonization time, power consumption height, utilization rate of carbon dioxide is low, process should not control, product granularity is big, distribution model
The deficiencies of enclosing width.Although high-gravity carbonation method is dynamic method, fundamentally enhance the transmittance process of reactor and microcosmic mixing
Process.But there are the deficiencies of complicated for operation, power consumption is too big.
The content of the invention
The problems such as big, utilization rate of carbon dioxide is low are consumed for existing dynamic method, the present invention provides a kind of dynamic carbonizatin method
The method for producing calcium carbonate.
And the device the present invention also provides a kind of dynamic carbonizatin method production calcium carbonate.
To achieve the above object of the invention, the embodiment of the present invention employs following technical solution：
A kind of method of dynamic carbonizatin method production calcium carbonate, the method include at least following steps：
Step 1: suspension /V one is equipped with reaction chamber, downward opening dynamic response device in retort, to the reaction
Tank adds in the Ca (OH) of allotment2Slurry, and submerge the opening of the dynamic response device；
Step 2: the Ca (OH) in the retort is extracted by reflux pump2Slurry, and to the dynamic response device
Reaction chamber in spray reflux；
Meanwhile it is passed through into the reaction chamber containing CO2Mixed gas；
Step 3: monitoring the pH value of the reaction paste in the retort, when pH value is 7-8, stop backflow of slurry, system
Obtain calcium carbonate crude product.
The method of dynamic carbonizatin method production calcium carbonate provided by the invention has the advantage that：
Reflux pump is by Ca (OH)2Slurry circulated sprinkling in retort adds in, and calcium hydroxide slurry is dispersed phase, and gas is
Continuous phase, greatly increase solution-air contact surface, extend droplet residence time in dynamic response device, also just extend gas-
Liquid time of contact, nucleus is quickly formed, be conducive to the progress of carburizing reagent, saved carbonization time；
The method of dynamic carbonizatin method provided by the invention production calcium carbonate, carbonization speed in the unit interval with producing calcium carbonate
Amount represent that prior art carbonization speed is 1.5t/h, present invention carbonization speed 2.4t/h now.Carbonization speed improves
60%.Carbonization time per ton shortens 0.25h, and carbonization time shortens 37.5%.2-4 microns of calcium carbonate superfine powder grain size is generated,
Less than 5 microns, and whiteness is up to 94.8.CO2 emissions are reduced, utilization rate of carbon dioxide is increased to by original 50%
69%.
Correspondingly, the present invention also provides a kind of devices of dynamic carbonizatin method production calcium carbonate, including retort, further include：
Dynamic response device, suspension /V is in the retort, the dynamic response device bottom end opening, and equipped with umbrella shape gas
Body distributor；
CO2Proportioner, for allocating CO2The volume content of gas, and pass through pipeline and connect with the dynamic response device upper end
It is logical；
Slurry return pipe, liquid feeding end with it is described reaction pot bottom refluxing opening connect, outlet end by reflux pump with it is described
The upper end connection of dynamic response device.
Compared with the prior art, the device of dynamic carbonizatin method production calcium carbonate provided by the invention, device is simple, and slurry returns
Calcium hydroxide slurry is carried out cycling addition by flow tube and reflux pump, and calcium hydroxide slurry is dispersed phase, and gas is continuous phase, significantly
Increase solution-air contact surface, extend droplet residence time in dynamic response device, also just extend solution-air time of contact,
It is quick to form nucleus, be conducive to the progress of carburizing reagent, save carbonization time；
Using in dynamic response device top and CO2Proportioner communicates, and allocates CO2The volume content of gas is conducive to reaction
It carries out, and CO2It is less than the reactor from lower part air inlet into device resistance, reduces power consumption, substantially reduce investment；On simultaneously
Portion's air inlet can increase the path of reaction in dynamic response device, save the carburizing reagent time；
Umbrella shape gas distributor is by CO2Gas uniformly sheds, and will not form air pocket, make CO2Gas and the hydrogen in retort
Calcium oxide carries out carburizing reagent again, and slurry return pipe causes calcium hydroxide slurry flowing always, is fully reacted, finally
Carbonization speed improves 60%, CO2Utilization rate improves 20%, is finally reached reduction energy consumption, effect easy to operate.
Description of the drawings
It to describe the technical solutions in the embodiments of the present invention more clearly, below will be to needed in the embodiment
Attached drawing is briefly described, it should be apparent that, the accompanying drawings in the following description is only some embodiments of the present invention, for ability
For the those of ordinary skill of domain, without creative efforts, it can also be obtained according to these attached drawings other attached
Figure.
Fig. 1 is dynamic carburizing reagent schematic device provided in an embodiment of the present invention；
Fig. 2 is umbrella shape gas distributor schematic top plan view provided in an embodiment of the present invention.
Wherein：11、CO2Bottle；12nd, air pump；13rd, flowmeter；14、CO2Proportioner；21st, retort；22nd, backflow of slurry
Pipe；23rd, pH measuring devices；24th, spray equipment；25th, dynamic response device；26th, umbrella shape gas distributor；27th, qi-emitting hole；28th, saw
Tooth；29th, reflux pump；30th, discharge port.
Specific embodiment
In order to make the purpose , technical scheme and advantage of the present invention be clearer, with reference to embodiments, to the present invention
It is further elaborated.It should be appreciated that the specific embodiments described herein are merely illustrative of the present invention, it is not used to
Limit the present invention.
A kind of method of dynamic carbonizatin method production calcium carbonate, the method include at least following steps：
Step 1: suspension /V one is equipped with reaction chamber, downward opening dynamic response device in retort, to the reaction
Tank adds in the Ca (OH) of allotment2Slurry, and submerge the opening of the dynamic response device；
Step 2: the Ca (OH) in the retort is extracted by reflux pump2Slurry, and to the dynamic response device
Reaction chamber in spray reflux；
Meanwhile it is passed through into the reaction chamber containing CO2Mixed gas；
Step 3: monitoring the pH value of the reaction paste in the retort, when pH value is 7-8, stop backflow of slurry, system
Obtain calcium carbonate crude product.
The method of dynamic carbonizatin method production calcium carbonate provided by the invention has the advantage that：
The method of dynamic carbonizatin method provided by the invention production calcium carbonate, carbonization speed in the unit interval with producing calcium carbonate
Amount represent that prior art carbonization speed is 1.5t/h, present invention carbonization speed 2.4t/h now.Carbonization speed improves
60%.Carbonization time per ton shortens 0.25h, and carbonization time shortens 37.5%.2-4 microns of calcium carbonate superfine powder grain size is generated,
Less than 5 microns, and whiteness is up to 94.8.CO2 emissions are reduced, utilization rate of carbon dioxide is increased to by original 50%
69%.
Preferably, in step 1, the Ca (OH)2The concentration of slurries is 8-10wt%, and temperature is 40-50 DEG C.
Ca(OH)2Influence of the concentration of slurry to calcium carbonate grain size：Ca(OH)2When concentration is relatively low, calcium carbonate grain size is smaller.When
Ca(OH)2After concentration is more than 10%, it is too fast that carbonization heat release so that system temperature rises, and carbonisation effectively in crystal growth, is made
Into the generation of big crystal, and since its system viscosity significantly increases, it is more serious to occur gel phenomenon in carbonisation, hinders
The movement of nucleus particle, provides condition, so that product particles become larger for the cohesion of particle；In addition, Ca (OH)2Concentration
Height, particle encounter during the reaction aggravate, and can also influence the stability of newly-generated calcium carbonate crystal so that calcium carbonate is brilliant
Grain is larger.
Ca(OH)2Influence of the concentration of slurry to the reaction time：With Ca (OH)2The increase of concentration, carburizing reagent time increase
Greatly.Ca(OH)2When concentration is relatively low, the denseness and viscosity of reaction system are smaller, the shadow of the increase Fluid Mechanics property of concentration
It rings less, the increasing degree in reaction time is smaller.Ca(OH)2Concentration is more than after certain value so that emulsion viscosity increases, particle fortune
It is dynamic slow, solid liquid interface liquid-film resistance increase, CO2Dissolving and mass transfer become difficult, so carbonization time extends.Improve Ca
(OH)2Although concentration is conducive to the progress of reaction, improve CO2Absorptivity.After concentration is more than 10%, there is gelatin phenomenon, to body
It is that the processes such as the three alternate mass transfer such as mixing, heat transfer and gas-liquid-solid of storeroom have a significant impact.The grain size of calcium carbonate substantially increases
Greatly, carbonization time also lengthens.But calcium hydroxide concentration can not be too low, equipment capacity can be caused to decline, in energy consumption
It rises, cost improves, and the waste water of generation is also more, and based on the above results, the suitable concentration of calcium hydroxide is 8-10% or so.
Preferably, in step 1, the Ca (OH)2The flow of slurries spray reflux is 35-40m3/h。
Ca(OH)2Influence of the flow of slurries spray reflux to calcium carbonate grain size：With Ca (OH)2The increase of slurry flow,
Influence for grain size is smaller, and carbonization time shortens, CO2Utilization rate is improved.CO2Throughput is very big, at Ca (OH)2Slurries
In the case of flow very little, Ca (OH)2Rate of dissolution is limited, CO2It is excessive.On the other hand, Ca (OH)2Slurry flow is small, to gas
Shearing force it is small, the bubble diameter into liquid phase is big, is unfavorable for mass transfer, therefore at Ca (OH)2CO when slurry flow is small2Profit
It is low with rate.Since carburizing reagent is intermittently operated, while increases fluid flow and mean to increase liquid circulation in the unit interval
Number increases with gas touch opportunity, and increase mass transfer surfaces product strengthens CO2Absorption, be conducive to shorten carbonization time.With
The increase of liquid phase flow, shearing force increase, bubble diameter reduce, while increase fluid flow and be equivalent to increase liquid spout stream
Speed is conducive to liquid refining as droplet, and grain size reduces with the increase of flow.Therefore production equipment power etc. is considered
Condition.
Preferably, in step 2, the mixed gas is air and CO2Mixing, wherein CO2Volume content be 25-
35%, the flow of the mixed gas is 40-50m3/min。
The change of mixed gas flow has an impact reaction time and calcium carbonate grain size：Mixed gas flow increases favourable gas
CO on liquid interface2The increase of equilibrium concentration increases, strengthening transfer process, gas-liquid contact face from gas phase to the mass transfer rate of liquid phase
Product is big, shortens the reaction time.Because carburizing reagent is carried out at boundary, increase gas flow can increase solution-air and connect
Contacting surface is accumulated, the progress of accelerated carbonation reaction.But gas flow is excessive, gas liquid interfacial area is held essentially constant, gas not by
Scattered just escaped in the liquid phase is not engaged in reacting.Even if continuing to increase gas flow, CO will not be obviously improved2With
Gas-liquid mass transfer between liquid phase, reaction can make CO2Utilization rate reduces, therefore the reaction time is basically unchanged.CO2The increase of flow makes
Reaction rate is accelerated, and the substantial amounts of nucleus of moment generation, makes the calcium carbonate degree of supersaturation of generation increase in liquid phase, and grain size reduces, with
The progress of reaction, nucleus is grown to crystal grain with nucleus by constantly colliding, when the growth rate of nucleus is more than the life of nucleus
During into rate, obtained particle is larger.
Preferably, the openend of the dynamic response device is equipped with umbrella shape gas distributor, and base border is equipped with sawtooth.Institute
It states umbrella shape gas distributor to be immersed in below the liquid level of reaction paste, and umbrella shape gas distributor is equipped with qi-emitting hole, qi-emitting hole
Aperture be 0.8-1.5cm, spacing 1.5-2cm.
Umbrella shape gas distributor is by CO2Gas uniformly sheds, and will not form air pocket, make CO2Gas and the hydrogen in retort
Calcium oxide carries out carburizing reagent again, and slurry return pipe causes calcium hydroxide slurry flowing always, is fully reacted, finally
Carbonization speed improves 60%, CO2Utilization rate improves 20%, is finally reached reduction energy consumption, effect easy to operate.
Further, the embodiment of the present invention provides a kind of device of dynamic carbonizatin method production calcium carbonate, including retort 21,
It further includes：
Dynamic response device 25, suspension /V is in the retort 21,25 bottom end opening of dynamic response device, and is equipped with
Umbrella shape gas distributor 26；
CO2Proportioner 14, for allocating CO2The volume content of gas, and pass through pipeline and 26 upper end of dynamic response device
Connection；
Slurry return pipe 22, liquid feeding end are connected with the refluxing opening of 21 bottom of retort, and outlet end passes through reflux pump 29
It is connected with the upper end of the dynamic response device 25.
Compared with the prior art, the device of dynamic carbonizatin method production calcium carbonate provided by the invention, device is simple, passes through slurry
Calcium hydroxide slurry is carried out cycling addition by material return duct 22 and reflux pump 29, and calcium hydroxide slurry is dispersed phase, and gas is company
Continuous phase greatly increases solution-air contact surface, extends droplet residence time in dynamic response device 25, also just extend gas-
Liquid time of contact, nucleus is quickly formed, be conducive to the progress of carburizing reagent, saved carbonization time；
Using in 25 top of dynamic response device and CO2Proportioner 14 communicates, CO2It is less than into device resistance from lower part air inlet
Reactor, reduce power consumption, substantially reduce investment；Top air inlet can increase the road of reaction in dynamic response device simultaneously
The carburizing reagent time is saved in footpath；
Umbrella shape gas distributor 26 is by CO2Gas uniformly sheds, and will not form air pocket, make CO2In gas and retort
Calcium hydroxide carries out carburizing reagent again, and slurry return pipe causes calcium hydroxide slurry flowing always, is fully reacted, most
Whole carbonization speed improves 60%, CO2Utilization rate improves 20%, is finally reached reduction energy consumption, effect easy to operate.
Preferably, 22 outlet end of slurry return pipe is equipped with spray equipment 24.The spray equipment 24 is to pass through threeway
3 connected spray heads of pipe, and spray head is equipped with the spray apertures that aperture is 1-2cm.
Calcium hydroxide slurry is formed high-speed jet by spray equipment 24, with CO2It comes into full contact with, increases CO2Utilization rate.Spray
The spray apertures aperture drenched on head is too small, easily blocks, too greatly, technique effect is not achieved.
Preferably, the CO2Proportioner 14 is equipped with air intlet, CO2Gas import and CO2Mixed gas outlet, the sky
Gas import is connected with the air outlet of air pump 12, the CO2Gas import and CO2Bottle 11 communicates, the CO2Mixed gas outlet leads to
Pipeline is crossed to connect with 25 upper end of dynamic response device.
Pass through CO in reaction process2Proportioner 14 matches CO2The suitable mixed gas of concentration is suitble to dynamic response method to prepare
Calcium carbonate.
Preferably, 21 side wall of retort is equipped with pH measuring devices 23,.
Preferably, 21 bottom of retort is equipped with discharge port 30.
It is provided in an embodiment of the present invention in order to better illustrate, it is illustrated below by embodiment is further.
Embodiment 1
The embodiment of the present invention provides a kind of device of dynamic carbonizatin method production calcium carbonate, refer to the attached drawing 1 and 2, including reaction
Tank 21, further includes：Dynamic response device 25, suspension /V is in the retort 21,25 bottom end opening of dynamic response device, and
Equipped with umbrella shape gas distributor 26；
CO2Proportioner 14, for allocating CO2The volume content of gas, and pass through pipeline and 26 upper end of dynamic response device
Connection；
Slurry return pipe 22, liquid feeding end are connected with the refluxing opening of 21 bottom of retort, and outlet end passes through reflux pump 29
It is connected with the upper end of the dynamic response device 25；
PH measuring devices 23, on 21 side wall of retort.
Above-mentioned 22 outlet end of slurry return pipe is equipped with spray equipment 24.The spray equipment 24 is connected by three-way pipe
3 spray heads, and spray head is equipped with the spray apertures that aperture is 1-2cm.
Above-mentioned CO2The air outlet and CO with air pump 14 respectively of proportioner 142Bottle 11 communicates, and CO2Proportioner 14, CO2Bottle
11st, flowmeter 13 and valve are additionally provided in air pump 12.
Above-mentioned umbrella shape gas distributor 26 is immersed in below the liquid level of reaction paste, and base border is equipped with sawtooth 28.Institute
Umbrella shape gas distributor 26 is stated equipped with qi-emitting hole, the aperture of qi-emitting hole 27 is 0.8-1.5cm, spacing 1.5-2cm.
Above-mentioned 21 bottom of retort is equipped with discharge port 30.
The embodiment of the present invention also provides a kind of method of dynamic carbonizatin method production calcium carbonate, is given birth to using above-mentioned dynamic carbonizatin method
The device of calcium carbonate is produced, is comprised the following steps：
Step 1: suspension /V one is equipped with reaction chamber, downward opening dynamic response device in retort, to the reaction
Tank adds in the Ca (OH) of allotment2Slurry, and the opening of the dynamic response device is submerged, wherein Ca (OH)2The temperature of slurries is 45
DEG C, Ca (OH)2The concentration of slurries is 8wt%；
Step 2: the Ca (OH) in the retort is extracted by reflux pump2Slurry, and to the dynamic response device
Reaction chamber in spray reflux, wherein Ca (OH)2The flow of slurries spray reflux is 40m3/h；
Meanwhile it is passed through into the reaction chamber of the dynamic response device containing CO2Mixed gas, wherein mixed gas throughput are
45m3/ min, CO in mixed gas2Volume content be 30%；
Step 3: monitoring the pH value of the reaction paste in the retort, when pH value is 7-8, stop backflow of slurry, system
Obtain calcium carbonate crude product.
The present embodiment is detected using calcium carbonate prepared by the method for dynamic carbonizatin method production calcium carbonate.Pass through laser
Particle size analyzer is analyzed, and product average grain diameter 2-4um, product cut size is uniform, narrowly distributing, stable quality.Content etc. reaches technical grade
Standard meets national product standard.
It is compared with the prior art：Theoretically often production 1t calcium carbonate need to consume pure CO2 0.44t。
In the prior art：CO in interval carbonizatin method2Utilization rate be only 50%, then produce 1t calcium carbonate need to consume it is pure
CO20.88t, kiln gas CO2Content is 30%, actual needs kiln gas 1960m3, the CO of carbonisation discharge2Quantity be 0.44t.
Using the method for dynamic carbonizatin method provided in this embodiment production calcium carbonate, then its CO2Utilization rate up to 69%,
Then actual production 1t calcium carbonate need to consume pure CO20.64t, kiln gas carbon dioxide content are 30%, actual needs kiln gas 1423m3。
So, the CO of carbonisation discharge2Quality be only 0.20t, a young discharge CO24363200m3, energy conservation and environmental protection, with fine
Social benefit.
Due to the method and apparatus using dynamic carbonizatin method production calcium carbonate, carbonization time is shortened, electricity consumption per ton is saved
11.4 degree of electricity, the 492480 degree of electricity of using electricity wisely in 1 year, often degree electricity is according to 0.78 yuan of calculating, 8.89 yuan, 1 year of ton cost reduction
380,000 yuan of saving expense, considerable benefit.
The foregoing is merely illustrative of the preferred embodiments of the present invention, is not intended to limit the invention, all essences in the present invention
Any modification, equivalent substitution or improvement made within refreshing and principle etc., should all be included in the protection scope of the present invention.
Claims (10)
- A kind of 1. method of dynamic carbonizatin method production calcium carbonate, it is characterised in that：The method includes at least following steps：Step 1: suspension /V one is equipped with reaction chamber, downward opening dynamic response device in retort, add to the retort Enter the Ca (OH) of allotment2Slurry, and submerge the opening of the dynamic response device；Step 2: the Ca (OH) in the retort is extracted by reflux pump2Slurry, and to the anti-of the dynamic response device Answer intracavitary spray reflux；Meanwhile it is passed through into the reaction chamber containing CO2Mixed gas；Step 3: monitoring the pH value of the reaction paste in the retort, when pH value is 7-8, stop backflow of slurry, carbon is made Sour calcium crude product.
- 2. the method for dynamic carbonizatin method production calcium carbonate as described in claim 1, it is characterised in that：It is described in step 1 Ca(OH)2The concentration of slurries is 8-10wt%, and temperature is 40-50 DEG C；And/orThe Ca (OH)2The flow of slurries spray reflux is 35-40m3/h。
- 3. the method for dynamic carbonizatin method production calcium carbonate as described in claim 1, it is characterised in that：It is described in step 2 Mixed gas is air and CO2Mixing, wherein CO2Volume content be 25-35%；And/orThe flow of the mixed gas is 40-50m3/min。
- 4. the method for dynamic carbonizatin method production calcium carbonate as described in claim 1, it is characterised in that：The dynamic response device Openend is equipped with umbrella shape gas distributor, and base border is equipped with sawtooth.
- 5. the method for dynamic carbonizatin method production calcium carbonate as claimed in claim 4, it is characterised in that：The umbrella shape gas distribution Device is immersed in below the liquid level of reaction paste, and umbrella shape gas distributor is equipped with qi-emitting hole, and the aperture of qi-emitting hole is 0.8- 1.5cm, spacing 1.5-2cm.
- 6. a kind of device of dynamic carbonizatin method production calcium carbonate, including retort, which is characterized in that further include：Dynamic response device, suspension /V is in the retort, the dynamic response device bottom end opening, and equipped with umbrella shape gas point Cloth device；CO2Proportioner, for allocating CO2The volume content of gas, and pass through pipeline and connected with the dynamic response device upper end；Slurry return pipe, liquid feeding end are connected with the refluxing opening of the reaction pot bottom, and outlet end passes through reflux pump and the dynamic The upper end connection of reactor.
- 7. the device of dynamic carbonizatin method production calcium carbonate as claimed in claim 6, it is characterised in that：The slurry return pipe goes out Liquid end is equipped with spray equipment.
- 8. the device of dynamic carbonizatin method production calcium carbonate as claimed in claim 7, it is characterised in that：The spray equipment is logical 3 spray heads that three-way pipe is connected are crossed, and spray head is equipped with the spray apertures that aperture is 1-2cm.
- 9. the device of dynamic carbonizatin method production calcium carbonate as claimed in claim 6, it is characterised in that：The CO2It is set on proportioner There are air intlet, CO2Gas import and CO2Mixed gas outlet, the air intlet are connected with the air outlet of air pump, the CO2 Gas import and CO2Bottle communicates, the CO2Mixed gas outlet is connected by pipeline with the dynamic response device upper end.
- 10. the device of dynamic carbonizatin method production calcium carbonate as claimed in claim 6, it is characterised in that：The reaction pot sidewall It is equipped with pH measuring devices.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711487518.2A CN108101091B (en) | 2017-12-30 | 2017-12-30 | Method and device for producing calcium carbonate by dynamic carbonization method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711487518.2A CN108101091B (en) | 2017-12-30 | 2017-12-30 | Method and device for producing calcium carbonate by dynamic carbonization method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108101091A true CN108101091A (en) | 2018-06-01 |
| CN108101091B CN108101091B (en) | 2020-05-12 |
Family
ID=62215148
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711487518.2A Expired - Fee Related CN108101091B (en) | 2017-12-30 | 2017-12-30 | Method and device for producing calcium carbonate by dynamic carbonization method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108101091B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110540226A (en) * | 2019-10-07 | 2019-12-06 | 浙江省建德市正发药业有限公司 | preparation method of high-density calcium carbonate powder |
| CN113173685A (en) * | 2021-05-06 | 2021-07-27 | 诸暨市鲁森机械有限公司 | Carbonization box for material recovery based on salt mud innocent treatment |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040108082A1 (en) * | 2002-12-09 | 2004-06-10 | Specialty Minerals (Michigan) Inc. | Filler-fiber composite |
| CN202657975U (en) * | 2012-05-28 | 2013-01-09 | 石家庄市苍山钙业有限公司 | Light calcium carbonate production classification diaphragm carbonization device |
| CN103738993A (en) * | 2013-12-04 | 2014-04-23 | 芜湖卓越纳米新材料有限公司 | Carbonation reactor of energy-efficient nano calcium carbonate and preparation method of energy-efficient nano calcium carbonate |
-
2017
- 2017-12-30 CN CN201711487518.2A patent/CN108101091B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040108082A1 (en) * | 2002-12-09 | 2004-06-10 | Specialty Minerals (Michigan) Inc. | Filler-fiber composite |
| CN202657975U (en) * | 2012-05-28 | 2013-01-09 | 石家庄市苍山钙业有限公司 | Light calcium carbonate production classification diaphragm carbonization device |
| CN103738993A (en) * | 2013-12-04 | 2014-04-23 | 芜湖卓越纳米新材料有限公司 | Carbonation reactor of energy-efficient nano calcium carbonate and preparation method of energy-efficient nano calcium carbonate |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110540226A (en) * | 2019-10-07 | 2019-12-06 | 浙江省建德市正发药业有限公司 | preparation method of high-density calcium carbonate powder |
| CN110540226B (en) * | 2019-10-07 | 2022-05-27 | 浙江省建德市正发药业有限公司 | Preparation method of high-density calcium carbonate powder |
| CN113173685A (en) * | 2021-05-06 | 2021-07-27 | 诸暨市鲁森机械有限公司 | Carbonization box for material recovery based on salt mud innocent treatment |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108101091B (en) | 2020-05-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN204973893U (en) | Nanometer brium carbonate carbonization reaction unit | |
| CN102228776A (en) | Method and apparatus for removing sulfur dioxide from sulfuric acid industrial tail gas, and for recovering sulfuric acid | |
| CN103738993A (en) | Carbonation reactor of energy-efficient nano calcium carbonate and preparation method of energy-efficient nano calcium carbonate | |
| CN108101091A (en) | A kind of method and apparatus of dynamic carbonizatin method production calcium carbonate | |
| CN205527942U (en) | Inner loop ozone catalytic unit | |
| CN104841346A (en) | Disc reactor for gas desorption of absorbents different in viscosity | |
| CN203408621U (en) | Acidic flue gas treatment system | |
| CN104891545B (en) | The carburizing reagent device and method that nano-calcium carbonate produces | |
| CN202070285U (en) | Device for removing sulfur dioxides in sulphuric acid industrial tail gas and recovering sulphuric acid | |
| CN204911455U (en) | Tympanic bulla oxidation reaction unit | |
| CN202594800U (en) | Ultrafine calcium carbonate carbonizing reactor capable of enhancing gas and liquid mixing | |
| CN207671702U (en) | A kind of reaction unit for dynamic carbonizatin method | |
| CN205575669U (en) | Preparation nano calcium carbonate's device | |
| CN202369409U (en) | Reactor for synthesizing nano calcium carbonate micro powder | |
| CN205077017U (en) | Biogas biological desulfurization system | |
| CN209536986U (en) | A kind of diamond recyclable device not discharging nitrogen oxide | |
| CN209602101U (en) | A kind of diamond recyclable device improving nitric acid utilization rate | |
| CN208757295U (en) | A kind of device of flue gas desulfurization | |
| CN207313153U (en) | A kind of calcium carbonate carbonators with circulating water | |
| CN203448107U (en) | Energy-saving carbonization reactor | |
| CN201343450Y (en) | Dedicated reactor for preparing manganese sulfate solution with leached pyrolusite from sulfur dioxide gas | |
| CN101456596B (en) | Reactor suitable for sulphur dioxide gas leach manganese dioxide ore | |
| CN205650069U (en) | Desulfurizing tower system with improve structure oxidation unit | |
| CN109279602B (en) | Diamond recovery method, device and application for improving nitric acid utilization rate | |
| CN206051888U (en) | A kind of response system for preparing ethylene |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20200512 |