CN116119703A - Method for continuously producing strontium chloride solution - Google Patents
Method for continuously producing strontium chloride solution Download PDFInfo
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- CN116119703A CN116119703A CN202211089600.0A CN202211089600A CN116119703A CN 116119703 A CN116119703 A CN 116119703A CN 202211089600 A CN202211089600 A CN 202211089600A CN 116119703 A CN116119703 A CN 116119703A
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Abstract
The invention discloses a method for continuously producing strontium chloride solution, which not only overcomes the defects of poor environment, low stirring efficiency and the like of a discontinuous production method, but also improves the dispersion contact effect between reactants in a liquid stirring mode in a reaction tank and a separation tank, simultaneously separates strontium sulfate and strontium carbonate impurities which do not participate in chemical reaction, limits the strontium sulfate and the strontium carbonate impurities in the middle and lower parts of the reaction tank and the separation tank, and intensively collects the strontium sulfate and the strontium carbonate impurities after being discharged and filtered by a belt filter; and the trapped CO is removed by a compressor 2 The gas is stored in a carbon dioxide storage tank, and the trapped CO can meet the requirements of safety, environmental protection and occupational health 2 The concentration is high, and the method can be used as a raw material for producing strontium carbonate, thereby realizing the comprehensive utilization of carbon capture; finally, by returning the strontium chloride solution to the reaction tank, the carrier effect of the water in the strontium chloride solution is utilized again, and the concentration of the strontium chloride solution obtained by production can be greatly improved.
Description
Technical Field
The invention relates to the technical field of strontium chloride solution production methods, in particular to a method for continuously producing strontium chloride solution.
Background
Strontium chloride is one of the inorganic salts, the most common strontium salt, and aqueous solutions are weakly acidic. Strontium chloride is a precursor for the preparation of other strontium compounds and is also used as a corrosion inhibitor for aluminum. Also, strontium chloride may be used as a pyrotechnic red colorant.
In the existing device for producing strontium chloride solution by using strontiate and dilute hydrochloric acid as raw materials, mechanical stirring cannot be generally used due to strong corrosiveness and serious abrasion of hydrochloric acid, compressed air stirring is generally adopted, and the operation can only be carried out by adopting a discontinuous production method. Such intermittent production formulaThe method has the following disadvantages: 1. the air stirring effect is poor and the efficiency is low; 2. the coarse grain separation method which does not participate in the reaction is behind; 3. the irregular positive pressure state appears, the volatilized hydrochloric acid and overflowed CO 2 And water vapor, which can cause the working environment to be unable to keep up with the requirements of safety, environmental protection and occupational health; 4. non-captured CO 2 And the air is dispersed into the atmosphere, so that the greenhouse effect of the atmosphere is also enhanced.
Therefore, there is an urgent need to devise a method for producing strontium chloride solution, which can completely solve a series of problems caused by intermittent production.
Disclosure of Invention
In order to solve the technical problems, the invention provides a method for continuously producing strontium chloride solution.
The technical scheme is as follows:
a method for continuously producing strontium chloride solution, which is characterized by comprising the following steps:
s1, simultaneously conveying process water output by a process water conveying pipeline, strontianite output by a strontianite conveying hopper, strontium chloride solution output by a first-stage filter press and filter residue washing water output by a second-stage filter press to a ball mill;
s2, grinding the mixture by a ball mill to obtain solid-containing slurry, and enabling the solid-containing slurry to flow into the reaction tank through a solid-containing slurry inlet at the upper part of the side wall of the reaction tank;
s3, pumping the dilute hydrochloric acid output by the dilute hydrochloric acid conveying pipeline, the strontium chloride solution output by the first-stage filter press, the filter residue washing water output by the second-stage filter press, the washing water output by the washing tower, the filtering water output by the ground tank and the reaction slurry output by the stirring fine slurry outlet at the upper part of the side wall of the reaction tank into a stirring liquid inlet at the bottom of the reaction tank at the same time;
s4, after the product slurry obtained by the reaction in the reaction tank flows out from a product slurry outlet in the middle of the side wall of the reaction tank, the product slurry flows into the separation tank through a separation tank feed inlet in the middle upper part of the side wall of the separation tank;
s5, strontium sulfate particle slurry in the reaction tank flows out from a first strontium sulfate slurry outlet at the lower part of the side wall of the reaction tank and flows to the belt filter, strontium sulfate particles filtered by the belt filter are conveyed to a first storage yard for storage, and filtering water filtered by the belt filter flows into a ground tank below the belt filter;
s6, pumping reactants without large particles in the separating tank into a reactant inlet at the bottom of the separating tank after flowing out from a circulating material outlet at the upper part of the side wall of the separating tank, mixing and stirring the reactant slurry flowing in from the reacting tank, washing and separating strontium sulfate particle slurry in the separating tank, flowing out from a second strontium carbonate slurry outlet at the lower part of the side wall of the separating tank, flowing to a belt filter, conveying strontium carbonate particles filtered by the belt filter to a first storage yard for storage, and flowing filtering water filtered by the belt filter into a ground tank below the belt filter;
s7, pumping strontium chloride slurry in the separating tank into a first-stage filter press for filter pressing through a product outlet at the middle lower part of the side wall of the separating tank, enabling one part of strontium chloride solution filtered by the first-stage filter press to flow into a strontium chloride solution storage tank, enabling the other part of the strontium chloride solution to flow into a ball mill of the step S1 and a reaction tank of the step S3, carrying out filter pressing on filter residues filtered by the first-stage filter press by a second-stage filter press, enabling filter residue washing water filtered by the second-stage filter press to flow into the ball mill of the step S1 and the reaction tank of the step S3, and conveying filter residues filtered by the second-stage filter press to a second storage yard;
s8, after carbon dioxide gas generated in the reaction tank is discharged from the exhaust port of the reaction tank at the top of the reaction tank and carbon dioxide gas generated in the separation tank is discharged from the exhaust port of the separation tank at the top of the separation tank, the carbon dioxide gas is firstly washed in a washing tower, and after washing, the carbon dioxide gas is pumped to a carbon dioxide storage tank for storage by a compressor, wherein process water output by a process water conveying pipeline is supplied to the washing tower.
Compared with the prior art, the invention has the beneficial effects that:
the method for continuously producing the strontium chloride solution by adopting the technical scheme realizes continuous production of the strontium chloride solution, overcomes the defects of poor environment, low stirring efficiency and the like of the intermittent production method, improves the dispersion contact effect between reactants in a liquid stirring mode in the reaction tank and the separation tank, and simultaneously can ensure that the strontium sulfate and the strontium carbonate which do not participate in chemical reactionSeparating impurities, limiting the impurities at the middle lower parts of the reaction tank and the separation tank, discharging the impurities, filtering the impurities by a belt filter, and collecting the impurities in a concentrated way; and the trapped CO is removed by a compressor 2 The gas is stored in a carbon dioxide storage tank, and the trapped CO can meet the requirements of safety, environmental protection and occupational health 2 The concentration is high, and the method can be used as a raw material for producing strontium carbonate, thereby realizing the comprehensive utilization of carbon capture; finally, by returning the strontium chloride solution to the reaction tank, the carrier effect of the water in the strontium chloride solution is utilized again, and the concentration of the strontium chloride solution obtained by production can be greatly improved.
Drawings
FIG. 1 is a logic block diagram of a method for continuously producing strontium chloride solution;
fig. 2 is a schematic diagram of a system for continuously producing strontium chloride solution.
Detailed Description
The invention is further described below with reference to examples and figures.
As shown in fig. 1 and 2, a method for continuously producing a strontium chloride solution, based on a system for continuously producing a strontium chloride solution, comprises the steps of:
s1, simultaneously conveying process water output by a process water conveying pipeline 1, strontianite output by a strontianite conveying hopper 3, strontium chloride solution output by a first-stage filter press 11 and filter residue washing water output by a second-stage filter press 12 to a ball mill 4. Namely: the process water, strontianite, strontium chloride solution and filter residue washing water are simultaneously sent to a ball mill 4 for one-pass grinding.
S2, grinding the mixture by the ball mill 4 to obtain solid-containing slurry, and enabling the solid-containing slurry to flow into the reaction tank 5 through a solid-containing slurry inlet 5a at the upper part of the side wall of the reaction tank 5. It should be noted that the solid-containing slurry can flow into the reaction tank 5 by using a natural inflow mode by utilizing the height difference, and can also be directly conveyed into the reaction tank 5 by adopting a wear-resistant pump.
S3, the dilute hydrochloric acid output by the dilute hydrochloric acid conveying pipeline 2, the strontium chloride solution output by the primary filter press 11, the filter residue washing water output by the secondary filter press 12, the washing water output by the washing tower 7, the filtering water output by the ground tank 14 and the reaction slurry output by the stirring fine slurry outlet 5b at the upper part of the side wall of the reaction tank 5 are pumped into the stirring liquid inlet 5c at the bottom of the reaction tank 5 at the same time. Namely: the dilute hydrochloric acid, the strontium chloride solution, the filter residue washing water, the filtering water and the reaction slurry are taken as stirring liquid together and pumped into the bottom of the reaction tank 5.
And S4, after the reaction in the reaction tank 5 is completed, the resultant slurry obtained from the reaction flows out from a resultant slurry outlet 5d in the middle of the side wall of the reaction tank 5, and flows into the separation tank 6 through a separation tank feed inlet 6a in the middle upper part of the side wall of the separation tank 6. It should be noted that the resultant slurry may be flowed into the knock-out pot 6 by natural inflow using the height difference, or may be pumped into the knock-out pot 6.
S5, strontium sulfate particle slurry in the reaction tank 5 flows out from a first strontium sulfate slurry outlet 5e at the lower part of the side wall of the reaction tank 5 and then flows to the belt filter 10, strontium sulfate particles filtered by the belt filter 10 are conveyed to a first storage yard 15 for storage, and filtering water filtered by the belt filter 10 flows into a ground tank 14 below the belt filter 10. It should be noted that strontium sulfate particles are among the particles that do not participate in the reaction.
S6, after reactants without large particles in the separating tank 6 flow out through a circulating material outlet 6b at the upper part of the side wall of the separating tank 6, the reactants are pumped into a reactant inlet 6c at the bottom of the separating tank 6, the products slurry flowing in from the reacting tank 5 is mixed and stirred, strontium sulfate particle slurry in the separating tank 6 is elutriated and separated, then flows out from a second strontium sulfate slurry outlet 6e at the lower part of the side wall of the separating tank 6 and flows to the belt filter 10, strontium sulfate particles filtered by the belt filter 10 are conveyed to a first storage yard 15 for storage, and filtering water filtered by the belt filter 10 flows into a ground tank 14 positioned below the belt filter 10. It should be noted that the strontium sulfate particles belong to particles which do not participate in the reaction, and the strontium sulfate particles can be used as raw materials for producing strontium sulfate for recycling.
And S7, pumping strontium chloride slurry in the separating tank 6 into a first-stage filter press 11 through a product outlet 6d at the middle lower part of the side wall of the separating tank 6, filtering by the first-stage filter press 11, enabling most of strontium chloride solution filtered by the first-stage filter press 11 to flow into a strontium chloride solution storage tank 13, enabling the other small part to flow into a ball mill 4 of the step S1 and a reaction tank 5 of the step S3, filtering filter residues filtered by the first-stage filter press 11 by a second-stage filter press 12, enabling filter residue washing water filtered by the second-stage filter press 12 to flow into the ball mill 4 of the step S1 and the reaction tank 5 of the step S3, and conveying filter residues filtered by the second-stage filter press 12 to a second storage yard 17. It is to be noted that the strontium chloride solution flowing into the strontium chloride solution storage tank 13 is more than the strontium chloride solution flowing to the ball mill 4 of step S1 and the reaction tank 5 of step S3, and the concentration of the produced strontium chloride solution can be increased by a magnitude of approximately 7% by the partial reflux of the strontium chloride solution. Wherein, the filter residues obtained by filtering the primary filter press 11 can be fed to the secondary filter press 12 in two ways: 1. the filter residue obtained by filtering by the first-stage filter press 11 is firstly mixed with the process water output by the process water conveying pipeline 1, then flows into the stirring tank 16 for stirring, and the mixed solution after stirring is pumped into the second-stage filter press 12 for filter pressing. 2. The filter residue sent out from the first filter residue outlet 11c is washed in countercurrent twice and then enters the second storage yard 17, and the second washing liquid is conveyed to the ball mill 4 and the reaction tank 5 through the pipeline. The two modes can fully wash the filter residue, dissolve the soluble matters, and replace the free strontium chloride solution carried in the filter residue, thereby further improving the recovery rate of the strontium chloride solution.
S8, after carbon dioxide gas generated in the reaction tank 5 is discharged from a reaction tank exhaust port 5f at the top of the reaction tank 5 and carbon dioxide gas generated in the separation tank 6 is discharged from a separation tank exhaust port 6f at the top of the separation tank 6, the carbon dioxide gas enters a washing tower 7 for washing, and after washing, the carbon dioxide gas is pumped to a carbon dioxide storage tank 9 for storage by a compressor 8, wherein process water output by a process water conveying pipeline 1 is supplied to the washing tower 7.
Referring to fig. 2, the system for continuously producing strontium chloride solution mainly comprises a process water conveying pipeline 1, a dilute hydrochloric acid conveying pipeline 2, a strontianite conveying hopper 3, a ball mill 4, a reaction tank 5, a separation tank 6, a washing tower 7, a compressor 8, a carbon dioxide storage tank 9, a belt filter 10, a primary filter press 11, a secondary filter press 12, a strontium chloride solution storage tank 13, a ground tank 14, a first storage yard 15 and a second storage yard 17.
The reaction tank 5 is provided with a solid slurry inlet 5a, a stirring fine slurry outlet 5b, a stirring liquid inlet 5c, a resultant slurry outlet 5d, a first strontium sulfate slurry outlet 5e and a reaction tank exhaust port 5f. Specifically speaking, the reaction tank 5 includes from the top down the retort head, retort cask portion and retort cone barrel portion that communicate in proper order, and retort cask portion is cask shape structure, and retort cone barrel portion is cone barrel shape structure, and retort gas vent 5f sets up at the top of retort head, contains solid thick liquid import 5a and stirs fine thick liquid export 5b and all sets up the upper portion at retort cask portion circumference lateral wall, and the product thick liquid export 5d sets up the lower part at retort cone barrel portion circumference lateral wall, and first strontium sulfate thick liquid export 5e sets up on retort cone barrel portion's circumference lateral wall, and stirring liquid import 5c sets up the bottom at retort cone barrel portion. In the case of a proper solid-liquid ratio, on the one hand, the slurry containing no or little solid particles in the upper part of the reaction tank 5, the hydrochloric acid solution, other products containing no solid particles, or water, etc. are introduced from the bottom of the reaction tank 5 by the pumping force of the first stirring pump 22 to form a flushing fluid upward, and a sufficient countercurrent contact is formed with the solid-containing slurry reactant introduced from the upper part of the reaction tank 5 to rapidly complete the chemical reaction to be performed; on the other hand, under the action of gravity, the relatively coarse solid is naturally limited at the middle lower part of the reaction tank 5 by utilizing the advantage that the dropping speed of the particles is higher than that of other particles, so that the fine particle slurry and the coarse particle slurry form natural layering, and the fine particles always float at the upper part of the reaction tank 5, thereby providing conditions for liquid stirring; meanwhile, the upward flushing fluid is used for continuously flushing the dispersed ore pulp, so that acidolysis reaction in the reaction tank 5 can be rapidly completed.
The separator tank 6 is provided with a separator tank feed port 6a, a circulating material outlet 6b, a reactant inlet 6c, a product outlet 6d, a second strontium sulfate slurry outlet 6e, and a separator tank exhaust port 6f. The separator tank 6 includes separator tank head, separator tank cask portion and separator tank cone barrel portion that from the top down communicates in proper order, and separator tank cask portion is cask shape structure, and separator tank cone barrel portion is cone barrel shape structure, and separator tank gas vent 6f sets up the top at the separator tank head, and circulation material export 6b sets up the upper portion at separator tank cask portion circumference lateral wall, and separator tank feed inlet 6a sets up the middle part at separator tank cask portion circumference lateral wall, and the resultant outlet 6d sets up the lower part at separator tank cask portion circumference lateral wall, and second strontium sulfate thick liquid export 6e sets up on separator tank cone barrel portion's circumference lateral wall, and reactant inlet 6c sets up the bottom at separator tank cone barrel portion. The reactant without large solid particles is led out from the upper part of the barrel part of the separating tank 6, pumped into the bottom of the separating tank, stirred and separated from the slurry flowing from the reaction tank 5, and simultaneously the large particles which do not participate in the reaction in the resultant slurry are naturally limited in the cone barrel part of the separating tank under the action of gravity and led out from the lower part of the cone barrel part of the separating tank, filtered and washed by the belt filter 10, the filter residues are temporarily stored in the first storage yard 15, and the strontium chloride solution is output from the lower part of the barrel part of the separating tank to the first filter press 11.
The washing tower 7 is provided with a washing water outlet 7a, a carbon dioxide inlet 7b, a carbon dioxide outlet 7c and a washing water inlet 7d. Specifically, the carbon dioxide outlet 7c is provided at the top of the scrubber 7, the scrubber water inlet 7d is provided at the upper portion of the circumferential side wall of the scrubber 7, the scrubber water inlet 7d is for supplying water to the scrubber spray device 7e in the scrubber 7, the process water delivery line 1 supplies water to the scrubber water inlet 7d, the scrubber water outlet 7a also supplies water to the scrubber water inlet 7d through the line, and the scrubber spray device 7e is provided high enough to be able to scrub the carbon dioxide gas more sufficiently. The carbon dioxide inlet 7b is provided at the middle lower portion of the circumferential side wall of the washing tower 7, and the washing water outlet 7a is provided at the lower portion of the circumferential side wall of the washing tower 7. Not only can sufficiently wash the carbon dioxide, but also can reuse the washing water and the hydrogen chloride gas dissolved therein so as to further improve the utilization rate of the dilute hydrochloric acid solution.
The first-stage filter press 11 is provided with a first filter pressing inlet 11b, a first filtrate outlet 11a, a first filter residue outlet 11c and a process water supplementing inlet 11d. The second-stage filter press 12 is provided with a second filter pressing inlet 12b, a second filtrate outlet 12a and a second filter residue outlet 12c.
The pipeline connecting the ball mill 4 and the solid slurry containing inlet 5a is provided with a pulp pump 21, the pipeline connected with the stirring liquid inlet 5c is provided with a first stirring pump 22, the pipeline connected with the reactant inlet 6c is provided with a second stirring pump 23, the pipeline connected with the washing water outlet 7a is provided with a circulating pump 24, and the pipeline connecting the product outlet 6d and the first-stage filter press 11 is provided with a first filter press pump 25.
The process water conveying pipeline 1, the strontianite conveying hopper 3, the first filtrate outlet 11a and the second filtrate outlet 12a can all feed to the ball mill feed inlet 4a of the ball mill 4 through pipelines, and the ball mill discharge outlet 4b of the ball mill 4 feeds to the solid-containing slurry inlet 5a through pipelines. The dilute hydrochloric acid delivery pipe 2, the first filtrate outlet 11a, the second filtrate outlet 12a, the washing water outlet 7a, the ground tank 14 and the stirring fine slurry outlet 5b are all fed to the stirring liquid inlet 5c through pipes, and the resultant slurry outlet 5d is fed to the separator tank feed inlet 6a through pipes. The recycle outlet 6b feeds the reactant inlet 6c via a conduit and the product outlet 6d feeds the first press inlet 11b via a conduit. The first strontium sulfate slurry outlet 5e and the second strontium sulfate slurry outlet 6e are both used for feeding the belt filter 10 through pipelines, filter residues obtained by filtering the belt filter 10 are conveyed to a first storage yard 15 for storage, and filtering water obtained by filtering the belt filter 10 flows into a ground tank 14 below the belt filter 10. The reaction tank exhaust port 5f and the separation tank exhaust port 6f are both fed to the carbon dioxide inlet 7b of the scrubber 7 through a pipeline, the scrubbing water outlet 7a is fed to the stirring liquid inlet 5c through a pipeline, the carbon dioxide outlet 7c is fed to the compressor 8 through a pipeline, and the compressor 8 is fed to the carbon dioxide storage tank 9 through a pipeline. The process water conveying pipeline 1 feeds the process water supplementing inlet 11d through a pipeline, a part of strontium chloride solution output by the first filtrate outlet 11a feeds the material to the ball mill feed inlet 4a and the stirring liquid inlet 5c through a pipeline, most of the strontium chloride solution output by the first filtrate outlet 11a feeds the material to the strontium chloride solution storage tank 13 through a pipeline, and the first filtrate outlet 11a feeds most of the strontium chloride solution to the strontium chloride solution storage tank 13. The filter residue output by the first filter residue outlet 11c is fed to the second filter pressing inlet 12b after being uniformly mixed by adding water, and the filter residue output by the second filter residue outlet 12c falls into the second storage yard 17 by gravity.
The first filter residue outlet 11c feeds the second filter pressing inlet 12b in the following two ways:
mode one:
a mixed water spray washing device 11e is arranged above the first filter residue outlet 11c, the mixed water spray washing device 11e is used for supplementing water with the process water supplementing inlet 11d, and the mixture of the filter residue sent out by the first filter residue outlet 11c and the process water is stirred by the stirring tank 16 and then pumped into the second filter pressing inlet 12b through the second filter pressing pump 26. The filter residue can be sufficiently washed by means of water mixing and stirring, so that the free strontium chloride solution is replaced, and the solution is returned to the ball mill 4 and the reaction tank 5 through the second filtrate outlet 12b, thereby further improving the utilization rate of carrier water in the strontium chloride solution and simultaneously preparing the high-concentration strontium chloride solution.
Mode two:
the filter residue sent out by the first filter residue outlet 11c enters the second storage yard 17 after being washed by countercurrent twice, and the second washing liquid is conveyed to the ball mill feed inlet 4a and the stirring liquid inlet 5c through pipelines. The filter residue can be sufficiently washed by the way of countercurrent washing for two times, so that soluble matters are dissolved, and the yield of the strontium chloride solution is improved.
Further, the process water conveying pipeline 1 supplies water to the belt filter 10 through a filtering water supply pipeline 18, the first strontium sulfate slurry outlet 5e is discharged to the belt filter 10 through a strontium sulfate discharge pipeline 19, the second strontium sulfate slurry outlet 6e is discharged to the belt filter 10 through a strontium sulfate discharge pipeline 20, the outlet of the filtering water supply pipeline 18 is close to the discharging end of the belt filter 10, and the outlet of the strontium sulfate discharge pipeline 19 and the outlet of the strontium sulfate discharge pipeline 20 are both positioned between the outlet of the filtering water supply pipeline 18 and the feeding end of the belt filter 10. The strontium sulfate slag is filtered to filter out the entrained strontium chloride solution, and then is sprayed and washed by the process water, so that the free strontium chloride solution entrained in the strontium sulfate slag is washed and replaced, and the recovery rate of the strontium chloride solution is further improved.
Further, foam traps are arranged in or outside the reaction tank exhaust port 5f and the separation tank exhaust port 6f, so that foam impurities and the like can be filtered out, and trapped CO can be further promoted 2 Concentration. And, the top of carbon dioxide storage tank 9 is connected with carbon dioxide delivery line 27, is convenient for external transport and utilization.
In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "clockwise", "counterclockwise", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings are merely for convenience in describing the present invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present invention.
In the present invention, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.
In the present invention, unless expressly stated or limited otherwise, a first feature "above" or "below" a second feature may include both the first and second features being in direct contact, as well as the first and second features not being in direct contact but being in contact with each other through additional features therebetween. Moreover, a first feature being "above," "over" and "on" a second feature includes the first feature being directly above and obliquely above the second feature, or simply indicating that the first feature is higher in level than the second feature. The first feature being "under", "below" and "beneath" the second feature includes the first feature being directly under and obliquely below the second feature, or simply means that the first feature is less level than the second feature.
Finally, it should be noted that the above description is only a preferred embodiment of the present invention, and that many similar changes can be made by those skilled in the art without departing from the spirit and scope of the invention as defined in the appended claims.
Claims (9)
1. A method for continuously producing a strontium chloride solution, comprising the steps of:
s1, simultaneously conveying process water output by a process water conveying pipeline (1), strontianite output by a strontianite conveying hopper (3), strontium chloride solution output by a first-stage filter press (11) and filter residue washing water output by a second-stage filter press (12) to a ball mill (4);
s2, grinding the mixture by a ball mill (4) to obtain solid-containing slurry, and enabling the solid-containing slurry to flow into the reaction tank (5) through a solid-containing slurry inlet (5 a) at the upper part of the side wall of the reaction tank (5);
s3, dilute hydrochloric acid output by a dilute hydrochloric acid conveying pipeline (2), strontium chloride solution output by a primary filter press (11), filter residue washing water output by a secondary filter press (12), washing water output by a washing tower (7), filtering water output by a ground tank (14) and reaction slurry output by a stirring fine slurry outlet (5 b) at the upper part of the side wall of a reaction tank (5) are pumped into a stirring liquid inlet (5 c) at the bottom of the reaction tank (5) at the same time;
s4, after the product slurry obtained by the reaction in the reaction tank (5) flows out from a product slurry outlet (5 d) in the middle of the side wall of the reaction tank (5), the product slurry flows into the separation tank (6) through a separation tank feed inlet (6 a) in the middle upper part of the side wall of the separation tank (6);
s5, strontium sulfate particle slurry in the reaction tank (5) flows out from a first strontium sulfate slurry outlet (5 e) at the lower part of the side wall of the reaction tank (5) and flows to the belt filter (10), strontium sulfate particles filtered by the belt filter (10) are conveyed to a first storage yard (15) for storage, and filtering water filtered by the belt filter (10) flows into a ground tank (14) below the belt filter (10);
s6, pumping reactants without large particles in the separating tank (6) into a reactant inlet (6 c) at the bottom of the separating tank (6) after flowing out through a circulating material outlet (6 b) at the upper part of the side wall of the separating tank (6), mixing and stirring the product slurry flowing in from the reacting tank (5), washing and separating strontium sulfate particle slurry in the separating tank (6), flowing out from a second strontium carbonate slurry outlet (6 e) at the lower part of the side wall of the separating tank (6), flowing to a belt filter (10), conveying strontium carbonate particles filtered by the belt filter (10) to a first storage yard (15) for storage, and flowing filtering water filtered by the belt filter (10) into a ground tank (14) below the belt filter (10);
s7, pumping strontium chloride slurry in the separating tank (6) into a first-stage filter press (11) for filter pressing through a product outlet (6 d) at the middle lower part of the side wall of the separating tank (6), enabling part of strontium chloride solution filtered by the first-stage filter press (11) to flow into a strontium chloride solution storage tank (13), enabling the other part of the strontium chloride solution to flow into a ball mill (4) of the step S1 and a reaction tank (5) of the step S3, enabling filter residues filtered by the first-stage filter press (11) to be filter-pressed by a second-stage filter press (12), enabling filter residue washing water filtered by the second-stage filter press (12) to flow into the ball mill (4) of the step S1 and the reaction tank (5) of the step S3, and conveying filter residues filtered by the second-stage filter press (12) to a second storage yard (17);
s8, after carbon dioxide gas generated in the reaction tank (5) is discharged from a reaction tank exhaust port (5 f) at the top of the reaction tank (5) and carbon dioxide gas generated in the separation tank (6) is discharged from a separation tank exhaust port (6 f) at the top of the separation tank (6), the carbon dioxide gas is firstly washed in a washing tower (7), and after the washing is completed, the carbon dioxide gas is pumped to a carbon dioxide storage tank (9) for storage by a compressor (8), wherein process water output by a process water conveying pipeline (1) is supplied to the washing tower (7).
2. A method for continuously producing a strontium chloride solution as defined in claim 1, wherein: in the step S7, filter residues obtained by filtering by the first-stage filter press (11) are mixed firstly, process water output by the process water conveying pipeline (1) flows into the stirring tank (16) for stirring, and the mixed solution after stirring is pumped into the second-stage filter press (12) for filter pressing.
3. A method for continuously producing a strontium chloride solution as defined in claim 1, wherein: in the step S7, the filter residue sent out from the first filter residue outlet (11 c) enters a second storage yard (17) after being subjected to countercurrent washing for two times, and the two washing liquids are conveyed to the ball mill (4) and the reaction tank (5) through pipelines.
4. A method for continuously producing a strontium chloride solution as defined in claim 1, wherein: in the step S7, more strontium chloride solution flows into the strontium chloride solution storage tank (13) than flows into the ball mill (4) of the step S1 and the reaction tank (5) of the step S3.
5. A method for continuously producing a strontium chloride solution as defined in claim 1, wherein: the washing tower (7) is provided with a washing water outlet (7 a), a carbon dioxide inlet (7 b), a carbon dioxide outlet (7 c) and a washing water inlet (7 d), wherein the carbon dioxide outlet (7 c) is arranged at the top of the washing tower (7) and is communicated with the compressor (8) through a pipeline, the washing water inlet (7 d) is arranged at the upper part of the circumferential side wall of the washing tower (7) and is communicated with the process water conveying pipeline (1) through a pipeline, the carbon dioxide inlet (7 b) is arranged at the middle lower part of the circumferential side wall of the washing tower (7) and is communicated with the reaction tank exhaust port (5 f) and the separation tank exhaust port (6 f) through a pipeline, and the washing water outlet (7 a) is arranged at the lower part of the circumferential side wall of the washing tower (7) and is communicated with the stirring liquid inlet (5 c) or the ball mill feed inlet (4 a) through a pipeline.
6. A method for continuously producing a strontium chloride solution as defined in claim 5, wherein: be equipped with ore pulp pump (21) on connecting ball mill (4) and the pipeline that contains solid thick liquid import (5 a), be equipped with first stirring pump (22) on the pipeline that is connected with stirring liquid import (5 c), be equipped with second stirring pump (23) on the pipeline that is connected with reactant entry (6 c), be equipped with circulating pump (24) on the pipeline that is connected with washing water export (7 a), be equipped with first filter-pressing pump (25) on the pipeline that connects product export (6 d) and first filter press (11), the filter residue that first filter press (11) were strained pumps into second filter press (12) through second filter-pressing pump (26).
7. A method for continuously producing a strontium chloride solution as defined in claim 1, wherein: the reaction tank (5) comprises a reaction tank sealing head, a reaction tank barrel part and a reaction tank cone barrel part which are sequentially communicated from top to bottom, the reaction tank barrel part is of a barrel-shaped structure, the reaction tank cone barrel part is of a cone barrel-shaped structure, a reaction tank exhaust port (5 f) is arranged at the top of the reaction tank sealing head, a solid slurry inlet (5 a) and a stirring fine slurry outlet (5 b) are arranged on the upper part of the circumferential side wall of the reaction tank barrel part, a product slurry outlet (5 d) is arranged on the lower part of the circumferential side wall of the reaction tank barrel part, a first strontium sulfate slurry outlet (5 e) is arranged on the circumferential side wall of the reaction tank cone barrel part, and a stirring liquid inlet (5 c) is arranged at the bottom of the reaction tank cone barrel part.
8. A method for continuously producing a strontium chloride solution as defined in claim 1, wherein: the separator tank (6) comprises a separator tank sealing head, a separator tank barrel part and a separator tank cone barrel part which are sequentially communicated from top to bottom, the separator tank barrel part is of a barrel-shaped structure, the separator tank cone barrel part is of a cone barrel-shaped structure, a separator tank exhaust port (6 f) is arranged at the top of the separator tank sealing head, a circulating material outlet (6 b) is arranged at the upper part of the circumferential side wall of the separator tank barrel part, a separator tank feeding port (6 a) is arranged in the middle of the circumferential side wall of the separator tank barrel part, a product outlet (6 d) is arranged at the lower part of the circumferential side wall of the separator tank barrel part, and a second strontium sulfate slurry outlet (6 e) is arranged on the circumferential side wall of the separator tank cone barrel part, and a reactant inlet (6 c) is arranged at the bottom of the separator tank cone barrel part.
9. A method for continuously producing a strontium chloride solution as defined in claim 1, wherein: the process water conveying pipeline (1) is used for supplying water to the belt filter (10) through the filtering water supply pipeline (18), the first strontium sulfate slurry outlet (5 e) is arranged to the belt filter (10) through the strontium sulfate discharge pipeline (19), the second strontium sulfate slurry outlet (6 e) is arranged to the belt filter (10) through the strontium sulfate discharge pipeline (20), the outlet of the filtering water supply pipeline (18) is close to the discharging end of the belt filter (10), and the outlet of the strontium sulfate discharge pipeline (19) and the outlet of the strontium sulfate discharge pipeline (20) are both positioned between the outlet of the filtering water supply pipeline (18) and the feeding end of the belt filter (10).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211089600.0A CN116119703A (en) | 2022-09-07 | 2022-09-07 | Method for continuously producing strontium chloride solution |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211089600.0A CN116119703A (en) | 2022-09-07 | 2022-09-07 | Method for continuously producing strontium chloride solution |
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| Publication Number | Publication Date |
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| CN116119703A true CN116119703A (en) | 2023-05-16 |
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|---|---|---|---|
| CN202211089600.0A Pending CN116119703A (en) | 2022-09-07 | 2022-09-07 | Method for continuously producing strontium chloride solution |
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| Country | Link |
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| CN (1) | CN116119703A (en) |
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- 2022-09-07 CN CN202211089600.0A patent/CN116119703A/en active Pending
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