CN105347703A - Calcium magnesium carbonate salt mine decomposition method - Google Patents
Calcium magnesium carbonate salt mine decomposition method Download PDFInfo
- Publication number
- CN105347703A CN105347703A CN201510881187.5A CN201510881187A CN105347703A CN 105347703 A CN105347703 A CN 105347703A CN 201510881187 A CN201510881187 A CN 201510881187A CN 105347703 A CN105347703 A CN 105347703A
- Authority
- CN
- China
- Prior art keywords
- magnesium carbonate
- calcium carbonate
- ore deposit
- reaction
- reactor
- 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
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P40/00—Technologies relating to the processing of minerals
- Y02P40/40—Production or processing of lime, e.g. limestone regeneration of lime in pulp and sugar mills
Abstract
The invention provides a calcium magnesium carbonate salt mine decomposition method which comprises the following steps: an ammonium salt solution is adopted to decompose calcium magnesium carbonate salt mine, the decomposition reaction is conducted in a series-connected multistage reactor or a tower-type reactor, heat carried by mixed gas generated by decomposition reaction of the ammonium salt solution and the calcium magnesium carbonate salt mine through heating are used as heat sources for recycling. According to the provided calcium magnesium carbonate salt mine decomposition method, through the introduction of the multistage countercurrent series-connected reaction kettle or the tower-type reactor, not only are the problems that a single-stage reaction kettle is large in water evaporation amount, the energy consumption is wasted, and ammonium carbonate is relatively low in concentration and unstable solved, but also the efficient and stable reaction of decomposition of the calcium magnesium carbonate salt mine by ammonium salt is realized, the energy consumption cost is reduced, and the method is energy-saving and economical.
Description
Technical field
The invention belongs to chemical production field, relate to a kind of decomposition method of calcium carbonate and magnesium carbonate ore deposit, be specifically related to a kind of method adopting ammonium salt decomposition calcium carbonate and magnesium carbonate ore deposit.
Background technology
Carbonate mine is widely distributed, wherein in the majority with calcium carbonate and magnesium carbonate mineral again.And the main existence form in calcium carbonate and magnesium carbonate ore deposit comprises Wingdale, calcite based on calcium carbonate, the magnesite based on magnesiumcarbonate, and not only comprised calcium carbonate but also comprised the rhombspar of magnesiumcarbonate.At present, divide in order to two large directions to the utilization of carbonate mine, one is the corresponding carbonate and then can obtain corresponding metal oxide again, as produced magnesiumcarbonate, magnesium oxide, Magnesium Carbonate Light 41-45, calcium carbonate, calcium oxide, calcium hydroxide etc. of directly purifying from carbonate mine; Second be that the production technique of carbonate mine and other production technique coupling are produced other compounds, as soda ash etc.
Publication number is the processing method that patent discloses a kind of producing high purity magnesium oxide with dolomite of CN102275957A, and the method comprises the following steps: rhombspar is dried and calcined finally obtain magnesium oxide product through fragmentation, calcining, digestion, filtration, carbonization, solid-liquid separation, pyrolysis, magnesium basic carbonate.
Publication number is that a kind of low-grade magnesite that patent discloses of CN103011630A produces high purity magnesium hydroxide and method of magnesium oxide, the main execution step of the method is as follows: calcined at 900 ~ 1100 DEG C by low-grade magnesite stone in calcining furnace, obtain the light-burned ore of magnesite and carbonic acid gas, reclaim carbonic acid gas, broken light-burned ore, low-grade magnesite leaches, purifies, separation coupling produce high purity magnesium hydroxide and magnesium oxide then to utilize ammonia-ammonium salt cyclic regeneration to realize.
Above two kinds of inventive methods all belong to the utilization of hot method carbonate ore, its common shortcoming is that the utilization to carbonate ore all have employed the method for dinectly bruning, consider that calcining temperature is about 1000 DEG C, coal-fired introducing can cause a series of situation affecting product quality to occur.Such as, because the carbonic acid gas produced in calcination process also needs to continue to utilize, so its purity must obtain certain guarantee.But, in actual calcination process, owing to being mingled with a large amount of dust and this kind of foreign gas of similar sulfurous gas in calcining kiln gas, carbonic acid gas must carry out impurity and purification process before use, this operation can increase technical process again undoubtedly, improves the cost of the finished product further.In addition, the calcining kiln body calcining this kind of ore used must possess certain scale, and the utilization ratio of the heat that its burning produces is just high, and therefore, this also just limits the handiness of this kind of activity in production.
Utilize the many disadvantages of carbonate mine to solve the above-mentioned hot method mentioned, the relative wet method of a kind of and hot method has utilized the method for carbonate mine to be carried out.This method has abandoned the mode of high-temperature calcination, then have employed two kinds of relatively gentle forms, and one is utilize spent acid and carbonate ore to react; Two is utilize ammonium salt solution and carbonate ore to react.
Patent as publication number CN86102539A discloses a kind of ammonium salt solution to decompose the method for magnesia or mineral powder of magnesite.Ammonia in reaction system is steamed constantly carrying out of realization response by control temperature by this method, but the larger problem that this reaction exists be ammonia leave leaving often also along with large water gaging, this also just result in two results, and one is that the concentration of the ammoniacal liquor obtained is lower; Two is need to evaporate a large amount of water quantitative ammonia for obtaining, and the energy consumption of reaction system can not effectively be cut down.The method also needs additionally to add sulfuric acid and bicarbonate of ammonia simultaneously, does not realize raw-material making full use of, the while of wasting, adds production cost.So, from real production angle, though this production method of ammonium salt decomposition carbonate mine exists certain feasibility in theory, a gratifying industrial practice result still can not obtained.
Summary of the invention
The shortcoming of prior art in view of the above, the object of the present invention is to provide a kind of decomposition method of calcium carbonate and magnesium carbonate ore deposit, by by multi-stage countercurrent reactors in series or tower reactor, realizes the decomposition in calcium carbonate and magnesium carbonate ore deposit; And utilize heat pump principle to reclaim thermal source, recycle heat is utilized, not only reduces the energy consumption of reaction system, and reach the object of cleaner production, there is technical process simple, significantly reduce the features such as production cost.
For achieving the above object and other relevant objects, the invention provides a kind of decomposition method of calcium carbonate and magnesium carbonate ore deposit, ammonium salt solution is adopted to decompose calcium carbonate and magnesium carbonate ore deposit, described decomposition reaction is carried out in the staged reactor or tower reactor of series connection, and is used as heat-source Cycles by the heat that the mixed gas that heating ammonium salt solution and calcium carbonate and magnesium carbonate ore deposit decompose generation carries.
Preferably, described decomposition reaction is carried out in the staged reactor of series connection, comprises the steps:
1) by slurry that calcium carbonate and magnesium carbonate ore deposit and ammonium salt solution are mixed to form, A reactor reaction is entered through A reactor opening for feed, discharged by reaction solution discharge port at the bottom of A reactor still, enter next stage reactor through next stage reactor feed mouth again and continue reaction, successively after plural serial stage reactor reaction, reaction solution discharge port extraction reaction solution and solid product at the bottom of final stage reactor still;
More preferably, in step 1) in, described calcium carbonate and magnesium carbonate ore deposit is calcium carbonate and magnesium carbonate breeze, and the particle diameter of described calcium carbonate and magnesium carbonate breeze is 10 μm ~ 1mm.
Further preferably, described calcium carbonate and magnesium carbonate breeze includes but are not limited to limestone powder, magnesite powder, ground dolomite.Most preferably, described calcium carbonate and magnesium carbonate breeze is selected from any one in limestone powder, magnesite powder, ground dolomite.
More preferably, in step 1) in, the ammonium salt aqueous solution of described ammonium salt solution to be concentration be 10wt% ~ saturated.The mass concentration of ammonium salt solution can be 10 ~ 15wt% or 15 ~ 20wt% or 20 ~ 25wt% or 25wt% ~ saturated.
More preferably, in step 1) in, described ammonium salt includes but are not limited to ammonium sulfate, ammonium chloride, ammonium nitrate.Further preferably, described ammonium salt is selected from any one in ammonium sulfate, ammonium chloride, ammonium nitrate.
More preferably, in step 1) in, described ammonium salt solution and calcium carbonate and magnesium carbonate ore deposit add proportioning, calculate by the mol ratio of calcium ions and magnesium ions in ammonium radical ion in ammonium salt solution and calcium carbonate and magnesium carbonate ore deposit, its mol ratio is NH
4 +: (Ca
2++ Mg
2+)=(3 ~ 2): 1.
More preferably, in step 1) in, the progression of the staged reactor of described series connection is 2 ~ 6 grades.
More preferably, in step 1) in, described reaction solution and solid product, after solid-liquid separation, as preparing the raw material of calcium-magnesium ratio compound for subsequent production.
More preferably, in step 1) in, the conversion rate control in described calcium carbonate and magnesium carbonate ore deposit is for being not less than 80%.When the low conversion rate in described calcium carbonate and magnesium carbonate ore deposit is in 80%, then reduce input speed and make transformation efficiency be greater than 80%.
Further preferably, described calcium carbonate and magnesium carbonate breeze transformation efficiency by the total amount of calcium ions and magnesium ions that records in reaction product at the bottom of final stage reactor still in the unit time and in the unit time the feed intake ratio of middle the total content of magnesium and calcium of calcium carbonate and magnesium carbonate calculate.Specifically calculate by following formula I:
2) by well heater, final stage reactor is heated, make step 1) in calcium carbonate and magnesium carbonate ore deposit in final stage reactor and ammonium salt solution react, decompose the mixed gas producing ammonia, carbonic acid gas and water, described mixed gas is discharged from the outlet of final stage reactor vapor, reversely successively enter upper level reactor, finally discharged by A reactor vapour outlet;
More preferably, step 2) in, the temperature of reaction of described final stage reactor is 140 DEG C ~ 220 DEG C, and pressure is 0.2 ~ 2.5Mpa.
More preferably, step 2) in, the gross weight of the mixed gas of discharging in A reactor vapour outlet is for benchmark, and in described mixed gas, the concentration of ammonia is 10 ~ 30wt%.The concentration of ammonia in described mixed gas, controls by regulating the flow velocity of mixed gas.
3) by step 2) in discharge mixed gas enter condenser shell by condenser vapor import, in the heat that mixed gas carries and condenser tube layer after media for heat exchange, water vapor in mixed gas becomes liquid phase water to discharge after condensation, and the ammonia in mixed gas, carbonic acid gas are discharged with gas phase;
More preferably, after the ammonia in described mixed gas, carbonic acid gas are discharged, for follow-up producing process.
More preferably, step 3) in, the cooling temperature of described condenser shell is 80 ~ 130 DEG C, and pressure is 0.1 ~ 2Mpa.
4) by step 3) described in medium after heat exchange, be vaporized into gas, increasing temperature and pressure is realized through vapour compressor, then after entering calcium carbonate and magnesium carbonate ore deposit in heater heats final stage reactor and ammonium salt solution, in well heater, be condensed into liquid phase stream from heater core after heat exchange, then be back to the use of condenser tube layer internal recycle.
More preferably, step 4) in, in described condenser tube, medium is stable chemical nature, and boiling point, between the liquid phase substance of 60 ~ 120 DEG C, includes but are not limited to hexanaphthene, normal heptane, water, butanols etc.
Further preferably, in described condenser tube, medium is selected from any one in hexanaphthene, normal heptane, water, butanols.
Most preferably, in described condenser tube, medium is water.
More preferably, step 4) in, described gas temperature after vapour compressor compression is higher than the temperature 5 ~ 50 DEG C of final stage reactor.
Preferably, described decomposition reaction is carried out in tower reactor, comprises the steps:
A) calcium carbonate and magnesium carbonate ore deposit is filled in reaction tower;
More preferably, steps A) in, the particle diameter in described calcium carbonate and magnesium carbonate ore deposit is 1 ~ 50mm.
More preferably, steps A) in, the height that described reaction tower is filled in described calcium carbonate and magnesium carbonate ore deposit is 5 ~ 50m.
More preferably, steps A) in, described calcium carbonate and magnesium carbonate ore deposit includes but are not limited to Wingdale, magnesite, rhombspar.Further preferably, described calcium carbonate and magnesium carbonate ore deposit is selected from any one in Wingdale, magnesite, rhombspar.
More preferably, steps A) in, described calcium carbonate and magnesium carbonate ore deposit is both as the raw material of reaction, and again as the filler of reaction tower, limit coronite is distilled, and in a reaction tower, realization response is synchronously carried out with distilling.
B) the tower top ammonium salt solution opening for feed of ammonium salt solution from reaction tower is passed into, be sprayed at uniformly on calcium carbonate and magnesium carbonate ore deposit and react, reaction solution discharge port extraction reaction solution at the bottom of tower;
More preferably, in step B) in, described ammonium salt solution is the ammonium salt aqueous solution of concentration 10wt% ~ saturated.The mass concentration of ammonium salt solution can be 10 ~ 15wt% or 15 ~ 20wt% or 20 ~ 25wt% or 25wt% ~ saturated.
More preferably, in step B) in, described ammonium salt includes but are not limited to ammonium sulfate, ammonium chloride, ammonium nitrate.Further preferably, described ammonium salt is selected from any one in ammonium sulfate, ammonium chloride, ammonium nitrate.
More preferably, in step B) in, described reaction solution is as preparing the raw material of calcium-magnesium ratio compound for subsequent production.More preferably, in step B) in, the conversion rate control of described ammonium salt solution is for being not less than 70%.The transformation efficiency of described ammonium salt solution is undertaken by regulating the flow of described ammonium salt solution, when the low conversion rate of described ammonium salt solution is in 70%, makes transformation efficiency be greater than 70% by the flow reducing ammonium salt solution.
Further preferably, the transformation efficiency of described ammonium salt solution, by collecting the mixed gas of reaction tower top in the unit time, by Kjeldahl nitrogen determination ammonia amount wherein, calculates with the ratio of the total amount of the middle ammonium radical ion that feeds intake of unit time betaine solution.Specifically calculate by following formula II:
C) heated at the bottom of reaction tower by well heater, calcium carbonate and magnesium carbonate ore deposit and ammonium salt solution are reacted, decompose the mixed gas producing ammonia, carbonic acid gas and water, discharge from overhead vapours outlet;
More preferably, in step C) in, the column bottom temperature of described reaction tower is 150 ~ 260 DEG C, and pressure is 0.5 ~ 5MPa.
More preferably, in step C) in, the gross weight of the mixed gas of discharging in overhead vapours outlet is for benchmark, and in described mixed gas, the concentration of ammonia is 10 ~ 30wt%.The concentration of ammonia in described mixed gas, controls by regulating the flow velocity of mixed gas.
D) by step C) in discharge mixed gas enter condenser shell by condenser vapor import, in the heat that mixed gas carries and condenser tube layer after media for heat exchange, water vapor in mixed gas becomes liquid phase water to discharge after condensation, and the ammonia in mixed gas, carbonic acid gas are discharged with gas phase;
More preferably, after the ammonia in described mixed gas, carbonic acid gas are discharged, for follow-up producing process.
More preferably, in step D) in, the cooling temperature of described condenser shell is 80 ~ 130 DEG C, and pressure is 0.1 ~ 2Mpa.
E) by step D) described in medium after heat exchange, be vaporized into gas, increasing temperature and pressure is realized through vapour compressor, then enter after at the bottom of heater heats reaction tower, in well heater, be condensed into liquid phase stream from heater core after heat exchange, then be back to the use of condenser tube layer internal recycle.
More preferably, in step e) in, in described condenser tube, medium is stable chemical nature, and boiling point, between the liquid phase substance of 60 ~ 120 DEG C, includes but are not limited to hexanaphthene, normal heptane, water, butanols etc.
Further preferably, in described condenser tube, medium is selected from any one in hexanaphthene, normal heptane, water, butanols.
Most preferably, in described condenser tube, medium is water.
More preferably, in step e) in, described gas temperature after vapour compressor compression is higher than column bottom temperature 5 ~ 50 DEG C.
As mentioned above, the decomposition method in a kind of calcium carbonate and magnesium carbonate ore deposit of the present invention, utilizes staged reactor cascade reaction or tower reactor reaction to be combined with heat pump, well achieves the decomposition in calcium carbonate and magnesium carbonate ore deposit, have following beneficial effect:
(1) decomposition method in a kind of calcium carbonate and magnesium carbonate ore deposit provided by the invention, by introducing multi-stage countercurrent cascade reaction still or tower reactor, the evaporated quantity of water not only solving the existence of single-stage reactor is large, and energy consumption is wasted, and carbon ammonium concentration is on the low side and the problem of instability; Also achieve the reaction of ammonium salt decomposition calcium carbonate and magnesium carbonate ore deposit efficient stable.
(2) decomposition method in a kind of calcium carbonate and magnesium carbonate ore deposit provided by the invention, owing to adopting multi-stage countercurrent cascade reaction still or tower reactor, can produce the steam of continous-stable, make the steady running of heat pump energy, thus ensures the stably manufactured of subsequent technique.
(3) decomposition method in a kind of calcium carbonate and magnesium carbonate ore deposit provided by the invention, utilizes heat pump principle to reclaim heat energy, and recycle heat is utilized, reduce heat-energy losses, reduce energy consumption cost, energy-conservation, economical.
Accompanying drawing explanation
Fig. 1 is shown as the plural serial stage reaction schematic diagram in ammonium salt decomposition calcium carbonate and magnesium carbonate ore deposit in the present invention, wherein, and 1: A reactor opening for feed; 2: reaction solution discharge port at the bottom of A reactor still; 3: reaction solution discharge port at the bottom of final stage reactor still; 4: final stage reactor vapor exports; 5: A reactor vapour outlet; 6: condenser vapor import.
Fig. 2 is shown as the tower reactor reaction schematic diagram decomposed in calcium carbonate and magnesium carbonate ore deposit in the present invention, wherein, 1, ammonium salt solution opening for feed; 2, reaction solution discharge port at the bottom of tower; 3, overhead vapours exports; 4, condenser vapor import.
Embodiment
Set forth the present invention further below in conjunction with specific embodiment, should be understood that these embodiments are only not used in for illustration of the present invention and limit the scope of the invention.
Below by way of specific specific examples, embodiments of the present invention are described, those skilled in the art the content disclosed by this specification sheets can understand other advantages of the present invention and effect easily.The present invention can also be implemented or be applied by embodiments different in addition, and the every details in this specification sheets also can based on different viewpoints and application, carries out various modification or change not deviating under spirit of the present invention.
Notice, in the following example, the concrete processing unit that indicates or device all adopt conventional equipment in this area or device; All force value and scope all refer to relative pressure.The calcium carbonate and magnesium carbonate ore deposit used in the following example is as Wingdale, magnesite, rhombspar, and ammonium salt, as ammonium sulfate, ammonium chloride, ammonium nitrate, is the conventional sample can bought from the market.The water used in the following example is tap water.
In addition should be understood that the one or more method stepss mentioned in the present invention do not repel and can also to there is additive method step or can also insert additive method step before and after described combination step between these steps clearly mentioned, except as otherwise noted; Will also be understood that, the relation that is connected between the one or more equipment/devices mentioned in the present invention is not repelled and can also to be there are other equipment/devices or can also insert other equipment/devices before and after described clustered aggregates/device between these two equipment/devices clearly mentioned, except as otherwise noted.And, except as otherwise noted, the numbering of various method steps is only the convenient tool differentiating various method steps, but not be ordering or the enforceable scope of restriction the present invention of restriction various method steps, the change of its relativeness or adjustment, when changing technology contents without essence, when being also considered as the enforceable category of the present invention.
Embodiment 1
The decomposition method in calcium carbonate and magnesium carbonate ore deposit, carries out, comprises the steps: in the staged reactor of series connection
(1) form slurry after the aqueous ammonium chloride solution that to get particle diameter be limestone powder and the concentration of 10-100 μm is 10wt% mixes, wherein, the mol ratio controlling calcium ions and magnesium ions in ammonium radical ion and limestone powder in aqueous ammonium chloride solution is NH
4 +: (Ca+Mg)=2:1.Slurry is entered A reactor reaction through A reactor opening for feed, discharged by reaction solution discharge port at the bottom of A reactor still, enter next stage reactor through next stage reactor feed mouth again and continue reaction, successively after 6 grades of tandem reactor reactions, reaction solution discharge port extraction calcium chloride solution and insolubles at the bottom of final stage reactor still, after solid-liquid separation, the calcium chloride solution obtained is as preparing the raw material of calcium cpd for subsequent production.In reaction process, the transformation efficiency controlling limestone powder is 80%.The transformation efficiency of limestone powder calculates by following formula I.
(2) heated final stage reactor by steam heater, the temperature of reaction controlling final stage reactor is 140 DEG C, and pressure is 0.2Mpa.Limestone powder in final stage reactor and aqueous ammonium chloride solution are reacted, decompose the mixed gas producing ammonia, carbonic acid gas and water, described mixed gas is discharged from the outlet of final stage reactor vapor, reversely successively enters upper level reactor, is finally discharged by A reactor vapour outlet.Meanwhile, by the concentration of ammonia in the flow rate control mixed gas of adjustment mixed gas, the concentration of ammonia in mixed gas, for benchmark, controls as 10wt% by the gross weight of the mixed gas of discharging in A reactor vapour outlet.
(3) mixed gas of being discharged by A reactor vapour outlet is entered condenser shell by condenser vapor import, the cooling temperature controlling condenser shell is 130 DEG C, and pressure is 2Mpa.Water vapor in mixed gas becomes liquid water to discharge after condensation, and the ammonia in mixed gas, carbonic acid gas are discharged with gas phase, for follow-up producing process.
(4) in condenser tube layer, medium is that hexanaphthene is vaporized into gas after heat exchange, makes the hexanaphthene gas temperature after compression be 145 DEG C through vapour compressor.Then after entering limestone powder in heater heats final stage reactor and aqueous ammonium chloride solution, in well heater, after heat exchange, be condensed into liquid phase flow of cyclohexane from heater core, then be back to condenser tube layer internal recycle and use.
In whole reaction process, reactant, by reacting in 6 grades of tandem reactors, can solve the problem that the evaporated quantity of water of single-stage reactor existence is large, become liquid water to discharge the water vapor condensation in reaction product, reduce energy consumption.In reaction process can effectively, stability contorting carbon ammonium concentration, thus realize the reaction of ammonium salt decomposition calcium carbonate and magnesium carbonate ore deposit efficient stable.Meanwhile, adopt 6 stage countercurrent tandem reactors, the steam of continous-stable can be produced, and recycle heat is utilized, reduce heat-energy losses, to reduce costs, energy-conservation.
Embodiment 2
The decomposition method in calcium carbonate and magnesium carbonate ore deposit, carries out, comprises the steps: in tower reactor
(1) be that the Wingdale of 1 ~ 5mm is filled in reaction tower by particle diameter, packing height is 5m, makes Wingdale both as the raw material of reaction, again as the filler of reaction tower.
(2) be that the aqueous ammonium nitrate solution of 10wt% passes into from the tower top ammonium salt solution opening for feed of reaction tower by concentration, be sprayed at uniformly on Wingdale and react, reaction solution discharge port extraction ca nitrate soln at the bottom of tower, as preparing the raw material of calcium cpd for subsequent production.Meanwhile, by regulating the flow of aqueous ammonium nitrate solution, the transformation efficiency controlling aqueous ammonium nitrate solution is 70%.The transformation efficiency of described aqueous ammonium nitrate solution calculates by following formula II.
(3) heated at the bottom of reaction tower by steam heater, controlling column bottom temperature is 150 DEG C, and pressure is 0.5MPa, and Wingdale and aqueous ammonium nitrate solution are reacted, and decomposes the mixed gas producing ammonia, carbonic acid gas and water, discharges from overhead vapours outlet.Meanwhile, by the concentration of ammonia in the flow rate control mixed gas of adjustment mixed gas, the concentration of ammonia in mixed gas, for benchmark, controls as 10wt% by the gross weight of the mixed gas of discharging in overhead vapours outlet.
(4) mixed gas that overhead vapours outlet is discharged is entered condenser shell by condenser vapor import, the cooling temperature controlling condenser shell is 130 DEG C, and pressure is 2Mpa.Water vapor in mixed gas becomes liquid water to discharge after condensation, and the ammonia in mixed gas, carbonic acid gas are discharged with gas phase, for follow-up producing process.
(5) in condenser tube layer, medium is that hexanaphthene is vaporized into gas after heat exchange, makes the hexanaphthene gas temperature after compression be 155 DEG C through vapour compressor.Then enter after at the bottom of heater heats reaction tower, hexanaphthene gas is condensed into liquid phase flow of cyclohexane from heater core in well heater after heat exchange, then is back to the use of condenser tube layer internal recycle.
In whole reaction process, reactant, by reacting in tower reactor, can solve the problem that the evaporated quantity of water of single-stage reactor existence is large, become liquid water to discharge the water vapor condensation in reaction product, reduce energy consumption.In reaction process can effectively, stability contorting carbon ammonium concentration, thus realize the reaction of ammonium salt decomposition calcium carbonate and magnesium carbonate ore deposit efficient stable.Meanwhile, adopt tower reactor, can produce the steam of continous-stable, and recycle heat is utilized, minimizing heat-energy losses, reduces costs, energy-conservation.
Embodiment 3
The decomposition method in calcium carbonate and magnesium carbonate ore deposit, carries out, comprises the steps: in the staged reactor of series connection
(1) slurry is formed after the ammonium sulfate solution that to get particle diameter be magnesite powder and the concentration of 0.1 ~ 1mm is 20wt% mixes, wherein, the mol ratio NH of calcium ions and magnesium ions in ammonium root and magnesite powder in ammonium sulfate solution
4 +: (Ca+Mg)=3:1.Slurry is entered A reactor reaction through A reactor opening for feed, discharged by reaction solution discharge port at the bottom of A reactor still, enter second reactor through second reactor opening for feed again and continue reaction, reaction solution discharge port extraction reaction product Adlerika and insolubles at the bottom of second reactor still, after solid-liquid separation, the Adlerika obtained is as preparing the raw material of magnesium compound for subsequent production.In reaction process, the transformation efficiency controlling magnesite powder is 98%.The transformation efficiency of magnesite powder calculates by following formula I.
(2) heated final stage reactor by steam heater, the temperature of reaction controlling final stage reactor is 220 DEG C, and pressure is 2.5Mpa.Magnesite powder in final stage reactor and sulfation aqueous ammonium are reacted, decompose the mixed gas producing ammonia, carbonic acid gas and water, described mixed gas is discharged from the outlet of final stage reactor vapor, reversely enters A reactor, is finally discharged by A reactor vapour outlet.Meanwhile, by the concentration of ammonia in the flow rate control mixed gas of adjustment mixed gas, the concentration of ammonia in mixed gas, for benchmark, controls as 30wt% by the gross weight of the mixed gas of discharging in A reactor vapour outlet.
(3) mixed gas of being discharged by A reactor vapour outlet is entered condenser shell by condenser vapor import, the cooling temperature controlling condenser shell is 80 DEG C, and pressure is 0.1Mpa.Water vapor in mixed gas becomes liquid water to discharge after condensation, and the ammonia in mixed gas, carbonic acid gas are discharged with gas phase, for follow-up producing process.
(4) in condenser tube layer, medium is that water is vaporized into gas through heat exchange, makes the steam temperature after compression be 190 DEG C through vapour compressor.Then after entering magnesite stone flour in heater heats final stage reactor and ammoniumsulphate soln, in well heater, after heat exchange, be condensed into liquid phase water flow out well heater, then be back to condenser tube layer internal recycle and use.
In whole reaction process, reactant, by reacting in 2 grades of tandem reactors, can solve the problem that the evaporated quantity of water of single-stage reactor existence is large, become liquid water to discharge the water vapor condensation in reaction product, reduce energy consumption.In reaction process can effectively, stability contorting carbon ammonium concentration, thus realize the reaction of ammonium salt decomposition calcium carbonate and magnesium carbonate ore deposit efficient stable.Meanwhile, adopt 2 stage countercurrent tandem reactors, the steam of continous-stable can be produced, and recycle heat is utilized, reduce heat-energy losses, to reduce costs, energy-conservation.
Embodiment 4
The decomposition method in calcium carbonate and magnesium carbonate ore deposit, carries out, comprises the steps: in the staged reactor of series connection
(1) getting particle diameter is form slurry after the ground dolomite of 50-500 μm mixes with saturated aqueous ammonium nitrate solution, wherein, and the mol ratio NH of calcium ions and magnesium ions in ammonium radical ion and ground dolomite in aqueous ammonium nitrate solution
4 +: (Ca+Mg)=2.5:1.Slurry is entered A reactor reaction through A reactor opening for feed, discharged by reaction solution discharge port at the bottom of A reactor still, enter next stage reactor through next stage reactor feed mouth again and continue reaction, successively after 4 grades of tandem reactor reactions, reaction solution discharge port extraction magnesium nitrate solution, ca nitrate soln and insolubles at the bottom of final stage reactor still, after solid-liquid separation, magnesium nitrate solution and ca nitrate soln are as preparing the raw material of calcium-magnesium ratio compound for subsequent production.In reaction process, the transformation efficiency controlling ground dolomite is 90%.The transformation efficiency of ground dolomite calculates by following formula I.
(2) heated final stage reactor by steam heater, the temperature of reaction controlling final stage reactor is 180 DEG C, and pressure is 1.5Mpa.Ground dolomite in final stage reactor and aqueous ammonium nitrate solution are reacted, decompose the mixed gas producing ammonia, carbonic acid gas and water, described mixed gas is discharged from the outlet of final stage reactor vapor, reversely successively enters upper level reactor, is finally discharged by A reactor vapour outlet.Meanwhile, by the concentration of ammonia in the flow rate control mixed gas of adjustment mixed gas, the concentration of ammonia in mixed gas, for benchmark, controls as 20wt% by the gross weight of the mixed gas of discharging in A reactor vapour outlet.
(3) mixed gas of being discharged by A reactor vapour outlet is entered condenser shell by condenser vapor import, the cooling temperature controlling condenser shell is 100 DEG C, and pressure is 1Mpa.Water vapor in mixed gas becomes liquid water to discharge after condensation, and the ammonia in mixed gas, carbonic acid gas are discharged with gas phase, for follow-up producing process.
(4) in condenser tube layer, medium is that water is vaporized into water vapour after heat exchange, makes the steam temperature after compression be 165 DEG C through vapour compressor.Then after entering ground dolomite in heater heats final stage reactor and ammonium nitrate solution, in well heater, after heat exchange, be condensed into liquid phase water flow out well heater, then be back to condenser tube layer internal recycle and use.In whole reaction process, reactant, by reacting in 4 grades of tandem reactors, can solve the problem that the evaporated quantity of water of single-stage reactor existence is large, become liquid water to discharge the water vapor condensation in reaction product, reduce energy consumption.In reaction process can effectively, stability contorting carbon ammonium concentration, thus realize the reaction of ammonium salt decomposition calcium carbonate and magnesium carbonate ore deposit efficient stable.Meanwhile, adopt 4 stage countercurrent tandem reactors, the steam of continous-stable can be produced, and recycle heat is utilized, reduce heat-energy losses, to reduce costs, energy-conservation.
Embodiment 5
The decomposition method in calcium carbonate and magnesium carbonate ore deposit, carries out, comprises the steps: in tower reactor
(1) be that the magnesite of 10 ~ 50mm is filled in reaction tower by particle diameter, the height of filling is 50m, described magnesite both as the raw material of reaction, again as the filler of reaction tower.
(2) be that the ammonium sulfate solution of 25wt% passes into from the tower top ammonium salt solution opening for feed of reaction tower by concentration, be sprayed at uniformly on magnesite and react, reaction solution discharge port extraction Adlerika at the bottom of tower, as preparing the raw material of magnesium compound for subsequent production.Meanwhile, by regulating the flow of ammonium sulfate solution, the transformation efficiency controlling aqueous ammonium chloride solution is 96%.The transformation efficiency of described aqueous ammonium chloride solution calculates by following formula II.
(3) be 260 DEG C by steam heater to computer heating control column bottom temperature at the bottom of reaction tower, pressure is 5MPa, and magnesite and ammonium sulfate solution are reacted, and decomposes the mixed gas producing ammonia, carbonic acid gas and water, discharges from overhead vapours outlet.Meanwhile, by the concentration of ammonia in the flow rate control mixed gas of adjustment mixed gas, the concentration of ammonia in mixed gas, for benchmark, controls as 30wt% by the gross weight of the mixed gas of discharging in overhead vapours outlet.
(4) mixed gas that overhead vapours outlet is discharged is entered condenser shell by condenser vapor import, the cooling temperature controlling condenser shell is 80 DEG C, and pressure is 0.1Mpa.Water vapor in mixed gas becomes liquid water to discharge after condensation, and the ammonia in mixed gas, carbonic acid gas are discharged with gas phase, for follow-up producing process.
(5) in condenser tube layer, medium is that water is vaporized into gas after heat exchange, makes the steam temperature after compression be 200 DEG C through vapour compressor.Then enter after at the bottom of heater heats reaction tower, water vapor is condensed into liquid phase water and flows out well heater in well heater after heat exchange, then is back to the use of condenser tube layer internal recycle.
In whole reaction process, reactant, by reacting in tower reactor, can solve the problem that the evaporated quantity of water of single-stage reactor existence is large, become liquid water to discharge the water vapor condensation in reaction product, reduce energy consumption.In reaction process can effectively, stability contorting carbon ammonium concentration, thus realize the reaction of ammonium salt decomposition calcium carbonate and magnesium carbonate ore deposit efficient stable.Meanwhile, adopt tower reactor, can produce the steam of continous-stable, and recycle heat is utilized, minimizing heat-energy losses, reduces costs, energy-conservation.
Embodiment 6
The decomposition method in calcium carbonate and magnesium carbonate ore deposit, carries out, comprises the steps: in tower reactor
(1) be that the rhombspar of 20 ~ 30mm is filled in reaction tower by particle diameter, packing height is 25m, described rhombspar both as the raw material of reaction, again as the filler of reaction tower.
(2) the tower top ammonium salt solution opening for feed of saturated aqueous ammonium chloride from reaction tower is passed into, be sprayed at uniformly on rhombspar and react, reaction solution discharge port extraction calcium chloride solution and magnesium chloride solution at the bottom of tower, as preparing the raw material of calcium-magnesium ratio compound for subsequent production.Meanwhile, by regulating the flow of aqueous ammonium chloride solution, the transformation efficiency controlling aqueous ammonium chloride solution is 85%.The transformation efficiency of described aqueous ammonium chloride solution calculates by following formula II.
(3) heated at the bottom of reaction tower by steam heater, controlling column bottom temperature is 200 DEG C, and pressure is 3MPa, and rhombspar and aqueous ammonium chloride solution are reacted again, and decomposes the mixed gas producing ammonia, carbonic acid gas and water, discharges from overhead vapours outlet., meanwhile, by the concentration of ammonia in the flow rate control mixed gas of adjustment mixed gas, the concentration of ammonia in mixed gas, for benchmark, controls as 20wt% by the gross weight of the mixed gas of discharging in overhead vapours outlet.
(4) mixed gas that overhead vapours outlet is discharged is entered condenser shell by condenser vapor import, the cooling temperature controlling condenser shell is 110 DEG C, and pressure is 1.5Mpa.Water vapor in mixed gas becomes liquid water to discharge after condensation, and the ammonia in mixed gas, carbonic acid gas are discharged with gas phase, for follow-up producing process.
(5) in condenser tube layer, medium is that water is vaporized into water vapour after heat exchange, makes the steam temperature after compression be 180 DEG C through vapour compressor.Then enter after at the bottom of heater heats reaction tower, water vapor is condensed into liquid phase water and flows out well heater in well heater after heat exchange, then is back to the use of condenser tube layer internal recycle.
In whole reaction process, reactant, by reacting in tower reactor, can solve the problem that the evaporated quantity of water of single-stage reactor existence is large, become liquid water to discharge the water vapor condensation in reaction product, reduce energy consumption.In reaction process can effectively, stability contorting carbon ammonium concentration, thus realize the reaction of ammonium salt decomposition calcium carbonate and magnesium carbonate ore deposit efficient stable.Meanwhile, adopt tower reactor, can produce the steam of continous-stable, and recycle heat is utilized, minimizing heat-energy losses, reduces costs, energy-conservation.
So the present invention effectively overcomes various shortcoming of the prior art and tool high industrial utilization.
Above-described embodiment is illustrative principle of the present invention and effect thereof only, but not for limiting the present invention.Any person skilled in the art scholar all without prejudice under spirit of the present invention and category, can modify above-described embodiment or changes.Therefore, such as have in art usually know the knowledgeable do not depart from complete under disclosed spirit and technological thought all equivalence modify or change, must be contained by claim of the present invention.
Claims (9)
1. the decomposition method in a calcium carbonate and magnesium carbonate ore deposit, ammonium salt solution is adopted to decompose calcium carbonate and magnesium carbonate ore deposit, it is characterized in that, described decomposition reaction is carried out in the staged reactor or tower reactor of series connection, and is used as heat-source Cycles by the heat that the mixed gas that heating ammonium salt solution and calcium carbonate and magnesium carbonate ore deposit decompose generation carries.
2. the decomposition method in calcium carbonate and magnesium carbonate ore deposit according to claim 1, is characterized in that, described decomposition reaction is carried out in the staged reactor of series connection, comprises the steps:
1) by slurry that calcium carbonate and magnesium carbonate ore deposit and ammonium salt solution are mixed to form, A reactor reaction is entered through A reactor opening for feed, discharged by reaction solution discharge port at the bottom of A reactor still, enter next stage reactor through next stage reactor feed mouth again and continue reaction, successively after plural serial stage reactor reaction, reaction solution discharge port extraction reaction solution and solid product at the bottom of final stage reactor still;
2) by well heater, final stage reactor is heated, make step 1) in calcium carbonate and magnesium carbonate ore deposit in final stage reactor and ammonium salt solution react, decompose the mixed gas producing ammonia, carbonic acid gas and water, described mixed gas is discharged from the outlet of final stage reactor vapor, reversely successively enter upper level reactor, finally discharged by A reactor vapour outlet;
3) by step 2) in discharge mixed gas enter condenser shell by condenser vapor import, in the heat that mixed gas carries and condenser tube layer after media for heat exchange, water vapor in mixed gas becomes liquid phase water to discharge after condensation, and the ammonia in mixed gas, carbonic acid gas are discharged with gas phase;
4) by step 3) described in medium after heat exchange, be vaporized into gas, increasing temperature and pressure is realized through vapour compressor, then after entering calcium carbonate and magnesium carbonate ore deposit in heater heats final stage reactor and ammonium salt solution, in well heater, be condensed into liquid phase stream from heater core after heat exchange, then be back to the use of condenser tube layer internal recycle.
3. the decomposition method in calcium carbonate and magnesium carbonate ore deposit according to claim 2, it is characterized in that, in step 1) in, described ammonium salt solution and calcium carbonate and magnesium carbonate ore deposit add proportioning, be calculated as NH by the mol ratio of calcium ions and magnesium ions in ammonium radical ion in ammonium salt solution and calcium carbonate and magnesium carbonate ore deposit
4 +: (Ca
2++ Mg
2+)=(3 ~ 2): 1.
4. the decomposition method in calcium carbonate and magnesium carbonate ore deposit according to claim 2, is characterized in that, in step 1) in, also to comprise any one of following condition or multinomial:
A1) described calcium carbonate and magnesium carbonate ore deposit is calcium carbonate and magnesium carbonate breeze, and the particle diameter of described calcium carbonate and magnesium carbonate breeze is 10 μm ~ 1mm;
A2) described calcium carbonate and magnesium carbonate breeze is selected from any one in limestone powder, magnesite powder, ground dolomite;
A3) described ammonium salt solution is the ammonium salt aqueous solution of concentration 10wt% ~ saturated;
A4) described ammonium salt is selected from any one in ammonium sulfate, ammonium chloride, ammonium nitrate;
A5) progression of the staged reactor of described series connection is 2 ~ 6 grades;
A6) conversion rate control in described calcium carbonate and magnesium carbonate ore deposit is for being not less than 80%.
5. the decomposition method in calcium carbonate and magnesium carbonate ore deposit according to claim 2, is characterized in that, in step 2), 3) or 4) in, to comprise any one of following condition or multinomial:
B1) temperature of reaction of described final stage reactor is 140 DEG C ~ 220 DEG C, and pressure is 0.2 ~ 2.5Mpa;
The gross weight of mixed gas of b2) discharging in A reactor vapour outlet is for benchmark, and in described mixed gas, the concentration of ammonia is 10 ~ 30wt%;
B3) cooling temperature of described condenser shell is 80 ~ 130 DEG C, and pressure is 0.1 ~ 2Mpa;
B4) in described condenser tube, medium is stable chemical nature, and boiling point is between the liquid phase substance of 60 ~ 120 DEG C;
B5) described vapor temperature after vapour compressor compression is higher than the temperature 5 ~ 50 DEG C of final stage reactor.
6. the decomposition method in calcium carbonate and magnesium carbonate ore deposit according to claim 1, is characterized in that, described decomposition reaction is carried out in tower reactor, comprises the steps:
A) calcium carbonate and magnesium carbonate ore deposit is filled in reaction tower;
B) the tower top ammonium salt solution opening for feed of ammonium salt solution from reaction tower is passed into, be sprayed at uniformly on calcium carbonate and magnesium carbonate ore deposit and react, reaction solution discharge port extraction reaction solution at the bottom of tower;
C) heated at the bottom of reaction tower by well heater, calcium carbonate and magnesium carbonate ore deposit and ammonium salt solution are reacted, decompose the mixed gas producing ammonia, carbonic acid gas and water, discharge from overhead vapours outlet;
D) by step C) in discharge mixed gas enter condenser shell by condenser vapor import, in the heat that mixed gas carries and condenser tube layer after media for heat exchange, water vapor in mixed gas becomes liquid phase water to discharge after condensation, and the ammonia in mixed gas, carbonic acid gas are discharged with gas phase;
E) by step D) described in medium after heat exchange, be vaporized into gas, increasing temperature and pressure is realized through vapour compressor, then enter after at the bottom of heater heats reaction tower, in well heater, be condensed into liquid phase stream from heater core after heat exchange, then be back to the use of condenser tube layer internal recycle.
7. the decomposition method in calcium carbonate and magnesium carbonate ore deposit according to claim 6, is characterized in that, steps A) in, to comprise any one of following condition or multinomial:
C1) described calcium carbonate and magnesium carbonate ore deposit is as the filler of reaction tower, and reaction is synchronously carried out with distilling;
C2) particle diameter in described calcium carbonate and magnesium carbonate ore deposit is 1 ~ 50mm;
C3) height of described reaction tower is filled in described calcium carbonate and magnesium carbonate ore deposit is 5 ~ 50m;
C4) described calcium carbonate and magnesium carbonate ore deposit is selected from any one in Wingdale, magnesite, rhombspar.
8. the decomposition method in calcium carbonate and magnesium carbonate ore deposit according to claim 6, is characterized in that, step B) in, to comprise any one of following condition or multinomial:
D1) described ammonium salt solution is the ammonium salt aqueous solution of concentration 10wt% ~ saturated;
D2) described ammonium salt is selected from any one in ammonium sulfate, ammonium chloride, ammonium nitrate;
D3) conversion rate control of described ammonium salt solution is for being not less than 70%.
9. the decomposition method in calcium carbonate and magnesium carbonate ore deposit according to claim 6, is characterized in that, step C), D) or E) in, to comprise any one of following condition or multinomial:
E1) column bottom temperature of described reaction tower is 150 ~ 260 DEG C, and pressure is 0.5 ~ 5MPa;
E2) export the gross weight of the mixed gas of discharging in overhead vapours for benchmark, in described mixed gas, the concentration of ammonia is 10 ~ 30wt%;
E3) cooling temperature of described condenser shell is 80 ~ 130 DEG C, and pressure is 0.1 ~ 2Mpa;
E4) in described condenser tube, medium is stable chemical nature, and boiling point is between the liquid phase substance of 60 ~ 120 DEG C;
E5) described vapor temperature after vapour compressor compression is higher than column bottom temperature 5 ~ 50 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510881187.5A CN105347703B (en) | 2015-12-03 | 2015-12-03 | A kind of decomposition method of calcium carbonate and magnesium carbonate ore deposit |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510881187.5A CN105347703B (en) | 2015-12-03 | 2015-12-03 | A kind of decomposition method of calcium carbonate and magnesium carbonate ore deposit |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105347703A true CN105347703A (en) | 2016-02-24 |
| CN105347703B CN105347703B (en) | 2017-07-28 |
Family
ID=55323798
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510881187.5A Active CN105347703B (en) | 2015-12-03 | 2015-12-03 | A kind of decomposition method of calcium carbonate and magnesium carbonate ore deposit |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105347703B (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106018751A (en) * | 2016-07-01 | 2016-10-12 | 山东科技大学 | Carbonate mineral dolomitization simulation study system and application method thereof |
| CN106477613A (en) * | 2016-12-12 | 2017-03-08 | 济南中昌成套设备工程有限公司 | A kind of liquid-solid reaction technique and its device |
| CN106629805A (en) * | 2016-10-17 | 2017-05-10 | 交城县三喜化工有限公司 | Method and device for producing calcium nitrate liquid |
| CN110777256A (en) * | 2019-11-27 | 2020-02-11 | 龙岩紫云化学科技有限公司 | Reaction tower, use method and method for extracting magnesium and/or calcium from magnesium and/or calcium carbonate ore |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN86102539A (en) * | 1986-10-15 | 1988-04-27 | 上海敦煌化工厂 | The no waste liquid manufacture method of Magnesium Carbonate Light 41-45 |
| CN1033975A (en) * | 1988-01-06 | 1989-07-19 | 重庆化学工业总公司职工大学 | Process for preparation of light magnesia by leaching magnesite with ammonium salts |
| CN1446751A (en) * | 2002-03-22 | 2003-10-08 | 丹东松元化学有限公司 | Technique for producing magnesium hydroxide and mangesia by using ammonia complete cycle method |
| CN104843756A (en) * | 2015-03-26 | 2015-08-19 | 龙岩紫云化学科技有限公司 | Decomposition method of carbonatite |
-
2015
- 2015-12-03 CN CN201510881187.5A patent/CN105347703B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN86102539A (en) * | 1986-10-15 | 1988-04-27 | 上海敦煌化工厂 | The no waste liquid manufacture method of Magnesium Carbonate Light 41-45 |
| CN1033975A (en) * | 1988-01-06 | 1989-07-19 | 重庆化学工业总公司职工大学 | Process for preparation of light magnesia by leaching magnesite with ammonium salts |
| CN1446751A (en) * | 2002-03-22 | 2003-10-08 | 丹东松元化学有限公司 | Technique for producing magnesium hydroxide and mangesia by using ammonia complete cycle method |
| CN104843756A (en) * | 2015-03-26 | 2015-08-19 | 龙岩紫云化学科技有限公司 | Decomposition method of carbonatite |
Non-Patent Citations (1)
| Title |
|---|
| 高卿: "白云石制备氢氧化镁联产高纯碳酸钙的研究", 《中国优秀硕士学位论文全文数据库 工程科技 I辑》 * |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106018751A (en) * | 2016-07-01 | 2016-10-12 | 山东科技大学 | Carbonate mineral dolomitization simulation study system and application method thereof |
| CN106629805A (en) * | 2016-10-17 | 2017-05-10 | 交城县三喜化工有限公司 | Method and device for producing calcium nitrate liquid |
| CN106629805B (en) * | 2016-10-17 | 2017-11-21 | 交城县三喜化工有限公司 | A kind of method and its device for producing calcium nitrate liquid |
| CN106477613A (en) * | 2016-12-12 | 2017-03-08 | 济南中昌成套设备工程有限公司 | A kind of liquid-solid reaction technique and its device |
| CN110777256A (en) * | 2019-11-27 | 2020-02-11 | 龙岩紫云化学科技有限公司 | Reaction tower, use method and method for extracting magnesium and/or calcium from magnesium and/or calcium carbonate ore |
| CN110777256B (en) * | 2019-11-27 | 2021-09-07 | 龙岩紫云化学科技有限公司 | Reaction tower, use method and method for extracting magnesium and/or calcium from magnesium and/or calcium carbonate ore |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105347703B (en) | 2017-07-28 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CA2973518C (en) | System and method for purifying and preparing high-purity vanadium pentoxide powder | |
| CA2973499C (en) | System and method for producing high-purity vanadium pentoxide powder | |
| CA2973491C (en) | System and method for preparing high-purity vanadium pentoxide powder | |
| CA2973511C (en) | System and method for purifying vanadium pentoxide | |
| US10112846B2 (en) | System and method for producing high-purity vanadium tetraoxide powder | |
| CN105347703A (en) | Calcium magnesium carbonate salt mine decomposition method | |
| CN104310428A (en) | Liquid ammonium nitrate production system and production method | |
| CN109835951A (en) | A kind of system and method for chloridising production powder vanadium | |
| CN109835950A (en) | A kind of system and method for vanadium resource cleaning chlorination production high purity vanadic anhydride | |
| CN103058245B (en) | Equipment and technology of calcium oxide producing with calcium sulfate | |
| CN104478514B (en) | A kind of utilization gas cleaning accessory substance prepares the thermo-compression evaporation technique of chemical fertilizer | |
| CN114082386B (en) | Device and method for semi-continuously synthesizing high-purity magnesium fluoride | |
| CN103159365B (en) | Method and device for increasing concentration of iron ions in artificial rutile mother solution | |
| CN203173931U (en) | Device for increasing concentration of iron ions in artificial rutile mother liquor | |
| CN103771473A (en) | Method for preparing small particle size Al2O3 powder |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |