CN111807390A - System for preparing high-purity magnesium oxide from magnesium chloride solution and using method thereof - Google Patents
System for preparing high-purity magnesium oxide from magnesium chloride solution and using method thereof Download PDFInfo
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- CN111807390A CN111807390A CN202010752709.2A CN202010752709A CN111807390A CN 111807390 A CN111807390 A CN 111807390A CN 202010752709 A CN202010752709 A CN 202010752709A CN 111807390 A CN111807390 A CN 111807390A
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- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 title claims abstract description 129
- 229910001629 magnesium chloride Inorganic materials 0.000 title claims abstract description 64
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 title claims abstract description 40
- 239000000395 magnesium oxide Substances 0.000 title claims abstract description 39
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 title claims abstract description 38
- 238000000034 method Methods 0.000 title claims description 19
- 238000010521 absorption reaction Methods 0.000 claims abstract description 82
- 239000000843 powder Substances 0.000 claims abstract description 55
- 238000005406 washing Methods 0.000 claims abstract description 55
- 238000001354 calcination Methods 0.000 claims abstract description 31
- 238000001694 spray drying Methods 0.000 claims abstract description 28
- 239000003513 alkali Substances 0.000 claims abstract description 15
- 239000000463 material Substances 0.000 claims abstract description 10
- 238000005507 spraying Methods 0.000 claims abstract description 9
- 238000004519 manufacturing process Methods 0.000 claims abstract description 6
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 44
- 239000007789 gas Substances 0.000 claims description 24
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims description 18
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims description 18
- DARFZFVWKREYJJ-UHFFFAOYSA-L magnesium dichloride dihydrate Chemical compound O.O.[Mg+2].[Cl-].[Cl-] DARFZFVWKREYJJ-UHFFFAOYSA-L 0.000 claims description 8
- 238000003860 storage Methods 0.000 claims description 8
- 239000007921 spray Substances 0.000 claims description 7
- 238000005086 pumping Methods 0.000 claims description 6
- 238000006243 chemical reaction Methods 0.000 claims description 4
- 238000002360 preparation method Methods 0.000 claims description 2
- 238000011084 recovery Methods 0.000 claims 1
- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 abstract 1
- 239000002253 acid Substances 0.000 abstract 1
- 239000000428 dust Substances 0.000 abstract 1
- 229960002337 magnesium chloride Drugs 0.000 description 42
- 239000000047 product Substances 0.000 description 25
- 239000000243 solution Substances 0.000 description 25
- 239000013078 crystal Substances 0.000 description 10
- 238000000197 pyrolysis Methods 0.000 description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 238000005201 scrubbing Methods 0.000 description 6
- 229910001868 water Inorganic materials 0.000 description 6
- MJMDTFNVECGTEM-UHFFFAOYSA-L magnesium dichloride monohydrate Chemical compound O.[Mg+2].[Cl-].[Cl-] MJMDTFNVECGTEM-UHFFFAOYSA-L 0.000 description 5
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 4
- 239000000347 magnesium hydroxide Substances 0.000 description 4
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 4
- 150000003839 salts Chemical class 0.000 description 4
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 3
- 239000012267 brine Substances 0.000 description 3
- 238000001035 drying Methods 0.000 description 3
- 150000004677 hydrates Chemical class 0.000 description 3
- 238000006703 hydration reaction Methods 0.000 description 3
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 description 3
- 229940050906 magnesium chloride hexahydrate Drugs 0.000 description 3
- DHRRIBDTHFBPNG-UHFFFAOYSA-L magnesium dichloride hexahydrate Chemical compound O.O.O.O.O.O.[Mg+2].[Cl-].[Cl-] DHRRIBDTHFBPNG-UHFFFAOYSA-L 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 239000011343 solid material Substances 0.000 description 3
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 239000001110 calcium chloride Substances 0.000 description 2
- 229910001628 calcium chloride Inorganic materials 0.000 description 2
- 238000005243 fluidization Methods 0.000 description 2
- 239000001095 magnesium carbonate Substances 0.000 description 2
- 229910000021 magnesium carbonate Inorganic materials 0.000 description 2
- 229940031958 magnesium carbonate hydroxide Drugs 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 239000012265 solid product Substances 0.000 description 2
- 241001131796 Botaurus stellaris Species 0.000 description 1
- 229910005260 GaCl2 Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical compound OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000008367 deionised water Substances 0.000 description 1
- 229910021641 deionized water Inorganic materials 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000012065 filter cake Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 1
- 150000004687 hexahydrates Chemical class 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 150000002681 magnesium compounds Chemical class 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000010409 thin film Substances 0.000 description 1
- 239000004408 titanium dioxide Substances 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F5/00—Compounds of magnesium
- C01F5/02—Magnesia
- C01F5/06—Magnesia by thermal decomposition of magnesium compounds
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
- C01B7/03—Preparation from chlorides
- C01B7/035—Preparation of hydrogen chloride from chlorides
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
Abstract
The invention discloses a system for preparing high-purity magnesium oxide by magnesium chloride solution, which comprises a magnesium chloride solution tank, a high-pressure pump, a concentration washing tower, a spraying high-pressure pump, a hot-blast stove, a spray drying tower, a cyclone powder collecting device, a dynamic calcining furnace, a finished product cyclone powder collecting device, a finished product material tank, a primary absorption tower, a primary circulating absorption pump, a primary cooler, a secondary absorption tower, a secondary circulating pump, a secondary cooler, a tertiary absorption tower, a tertiary circulating pump, a tertiary cooler, a high-pressure induced draft fan, an alkali liquor washing tank and a circulating washing pump, and respectively form a production tin and absorption system. And dust and acid pollution can be effectively prevented.
Description
Technical Field
The invention belongs to the field of magnesium oxide preparation, and particularly relates to a system for preparing high-purity magnesium oxide from a magnesium chloride solution and a using method thereof.
Background
Magnesium oxide exists in sea water, salt lake water, underground salt mine and the like in a large amount in nature, and exists in the form of a magnesium chloride aqueous solution. The magnesium chloride aqueous solution can crystallize hydrates of 2, 4, 6, 8 and 12 crystal waters, and the high hydrates are decomposed by heat to generate low hydrates. The hexahydrate is stable within the temperature range of-3.4 to 116.7 ℃. When the temperature exceeds 118 ℃, crystal water is lost, and hydrogen chloride gas is released to generate magnesium oxide.
The magnesium chloride is large in storage capacity and wide in distribution, and a large amount of brine produced in salt farms in provinces and provinces along the coast, underground salt brine in gulf regions are abundant, and inland salt lakes and underground brine are also abundant. The magnesium chloride not only has wide application, but also is an important raw material for preparing series products such as magnesium oxide, light magnesium carbonate, magnesium hydroxide and the like.
In many chemical engineering processes, a low-price metal oxide is required to adjust the pH value, when the prior environmental protection form is not too strict, calcium oxide is adopted to adjust the pH value to generate calcium chloride, and then a calcium chloride solution is dried to form a calcium chloride product. For example, in the "titanium dioxide by hydrochloric acid method" process, when the pH value is adjusted by magnesium oxide, the hydrochloric acid and magnesium oxide generate magnesium chloride, the magnesium chloride is decomposed into magnesium oxide and hydrochloric acid, the hydrochloric acid is returned to the system, and the magnesium oxide is reused for adjusting the pH value, so that the process forms a closed cycle process.
At present, the technological method for producing magnesium oxide by using magnesium chloride as a raw material mostly adopts a carbonic acid method, a carbonization method and an alkali method to convert the magnesium chloride into magnesium carbonate or magnesium hydroxide, and then calcines the magnesium carbonate or magnesium hydroxide to produce the magnesium oxide.
Application number 201510586630.6 discloses a method and a device for producing high-purity magnesium oxide and co-producing industrial concentrated hydrochloric acid by fluidization pyrolysis of low-hydration magnesium chloride, the method takes saturated magnesium chloride solution as a raw material, prepares magnesium chloride hexahydrate crystals by evaporative crystallization, and then dries the magnesium chloride hexahydrate crystals, so that the magnesium chloride hexahydrate crystals can not be hydrolyzed when dried, and low-hydration magnesium chloride particle materials containing 1-2 crystal water are obtained, the low-hydration magnesium chloride solid materials are subjected to fluidization pyrolysis in a fluidized bed pyrolysis furnace, and crude magnesium oxide and pyrolysis tail gas are obtained after gas-solid separation. As is well known, the fluidized bed has bed layer, only under the condition of positive pressure the gas can be passed through the material-loading layer of the bed to dry material, and under the normal condition the service temperature of industrial production fluidized bed is below 500 deg.C, if the electric heater is used as heat source, it is the highest cost heat source of drying and calcining equipment in China at present, and its cost is high, and its economic significance is not large, or the heat utilization rate of heat exchanger is low, and its economic significance is not large.
Application No.: 201410018911.7 discloses a method for preparing high-purity magnesium oxide from old bittern, which comprises drying magnesium chloride at 300 deg.C under 100 deg.C to remove part of crystal water, pyrolyzing at 750 deg.C under 550 deg.C to obtain magnesium oxide, wherein the drying equipment is fluidized drier, the pyrolyzing equipment is fluidized pyrolyzing furnace, the magnesium chloride undergoes pyrolysis reaction at 750 deg.C under 550 deg.C, the pyrolysis tail gas is directly contacted with cold magnesium chloride solid material through one-stage or multi-stage gas-solid cyclone separator, the pyrolysis tail gas is cooled, and the solid material is preheated. The pyrolysis solid product is directly contacted with cold air through a one-stage or multi-stage gas-solid cyclone separator, the pyrolysis solid product is cooled, and the cold air is preheated. The temperature parameters of the invention are elaborated in the book of magnesium compound production and application compiled by Huqingfu, magnesium chloride containing crystal water can form liquid under high temperature, if a cyclone preheater is adopted to preheat the crystal magnesium chloride, the crystal magnesium chloride is adhered to the cyclone preheater inevitably, and equipment can be blind in a short time.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides a system for preparing high-purity magnesium oxide from a magnesium chloride solution and a using method thereof.
In order to achieve the purpose, the invention adopts the following technical scheme:
a system for preparing high-purity magnesium oxide from magnesium chloride solution comprises a magnesium chloride solution tank, a high-pressure pump, a concentration washing tower, a spray high-pressure pump, a hot blast stove, a spray drying tower, a cyclone powder collector, a dynamic calcining furnace, a finished product cyclone powder collector, a finished product material tank, a primary absorption tower, a primary circulation absorption pump, a primary cooler, a secondary absorption tower, a secondary circulation pump, a secondary cooler, a tertiary absorption tower, a tertiary circulation pump, a tertiary cooler, a high-pressure induced draft fan, an alkali liquor washing tank and a circulation washing pump, wherein the high-pressure pump is connected to a pipeline between an outlet of the magnesium chloride solution tank and an inlet of the concentration washing tower, the spray high-pressure pump is connected to a pipeline between an inlet of the spray drying tower and an outlet of the concentration washing tower, an outlet of the spray drying tower is communicated with an inlet of the cyclone powder collector through a pipeline, an outlet of the cyclone powder collector is communicated with an inlet of, the air outlet of the hot blast stove is respectively communicated with the inlets of the spray drying tower, the cyclone powder collector and the dynamic calcining furnace through pipelines, the outlet of the dynamic calciner is connected with the inlet of a finished product cyclone powder collector, one outlet of the finished product cyclone powder collector is connected with the inlet of the spray drying tower through a pipeline, the other outlet is communicated with a finished product charging bucket through a pipeline, the magnesium chloride solution tank, the high-pressure pump, the concentration washing tower, the spraying high-pressure pump, the hot blast stove, the spray drying tower, the cyclone powder collector, the dynamic calcining furnace, the finished product cyclone powder collector and the finished product material tank form a production system, the absorption system consists of the first-stage absorption tower, the first-stage circulating absorption pump, the first-stage cooler, the second-stage absorption tower, the second-stage circulating pump, the second-stage cooler, the third-stage absorption tower, the third-stage circulating pump, the third-stage cooler, the high-pressure draught fan, the alkali liquor washing tank and the circulating washing pump.
Further, pass through the pipe connection in the export of concentrated scrubbing tower on absorption system, absorption system is including the one-level absorption tower, second grade absorption tower, the tertiary absorption tower that communicate in proper order, there are one-level cooler, second grade cooler, tertiary cooler in the export of one-level absorption tower, second grade absorption tower, tertiary absorption tower respectively pipe connection, the export of one-level cooler, second grade cooler, tertiary cooler is pipe connection one-level absorption tower, second grade absorption tower, tertiary absorption tower respectively, there is the concentrated hydrochloric acid storage tank in the export of one-level cooler still through the pipe connection, there is the high-pressure draught fan in the export of tertiary absorption tower through the pipe connection.
Furthermore, the export of high pressure draught fan has alkali lye washing tank through the pipe connection, communicate respectively in the export of alkali lye washing tank and have collection box and circulation scrubbing pump, the export of circulation scrubbing pump is linked together with alkali lye washing tank.
A use method of a system for preparing high-purity magnesium oxide from magnesium chloride solution comprises the following steps:
s1: pumping the magnesium chloride solution in the magnesium chloride solution pipe into a concentration washing tower through a high-pressure pump; concentrating in a concentrating washing tower and pumping into a spray drying tower by a spray high-pressure pump; meanwhile, the hot blast stove is opened, the dynamic calcining furnace is heated, the concentrated magnesium chloride solution in the spray drying tower reacts to obtain magnesium chloride dihydrate powder, and the magnesium chloride dihydrate powder is separated in a dry mode and a wet mode, then is sent into a cyclone powder collecting device and then is sent into the dynamic calcining furnace; the magnesium chloride dihydrate is calcined in a dynamic calcining furnace to generate magnesium chloride and hydrogen chloride gas, and then the magnesium chloride and the hydrogen chloride gas are collected by a finished product cyclone powder collector and finally sent into a finished product material pipe.
S2: when the step S1 is operated, the trace magnesium chloride solution generated by the cyclone powder collector is conveyed to the concentration washing tower again through the pipeline for standby, and the magnesium chloride dihydrate powder in the finished product cyclone powder collector is conveyed to the dynamic calcining furnace again through the pipeline for re-reaction;
s3: when the step S1 is operated, hydrogen chloride gas generated when the concentration washing tower works is sequentially conveyed to the first-stage absorption tower, the second-stage absorption tower and the third-stage absorption tower through pipelines to be absorbed, and is cooled by the first-stage cooler, the second-stage cooler and the third-stage cooler and finally input into the hydrochloric acid storage tank;
and S4, pumping the hydrogen chloride gas which is not absorbed by the three-stage absorption tower into an alkali liquor washing tank through a high-pressure induced draft fan and repeatedly absorbing the hydrogen chloride gas through a circulating washing pump when the operation is performed in the step S3.
Further, the high-pressure pump is regulated to output flow of 0.50-0.55 m through a valve for carrying out thin film cultivation.
Further, the outlet temperature of the hot blast stove is stabilized at 860 ℃, when the outlet temperature of the dynamic calcining tower reaches about 400 ℃, the spraying high-pressure pump is started to control the high-pressure flow, so that the temperature of the system is gradually increased, and when the outlet temperature of the dynamic calcining furnace reaches 500-530 ℃, the system enters a normal working state.
Further, the concentration of the magnesium chloride solution is 30% -40%.
By adopting the technical scheme, the invention has the beneficial effects that:
according to the invention, the magnesium oxide in the finished product tank is continuously washed by deionized water, the washed magnesium oxide can generate partial magnesium hydroxide, and the washed and filtered filter cake is calcined to obtain a high-purity magnesium oxide product with the magnesium oxide content of more than 99%, so that the produced magnesium oxide has high quality.
Drawings
Fig. 1 is a schematic structural view of the present invention.
Detailed Description
In order to make the technical means, the creation characteristics, the achievement purposes and the effects of the invention easy to understand, the invention is further explained by combining the specific embodiments as follows:
therefore, the following detailed description of the embodiments of the present invention, provided in the accompanying drawings, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention, and all other embodiments, which can be obtained by those skilled in the art based on the embodiments of the present invention without inventive faculty, are within the scope of the invention.
It should be noted that: like reference numbers and letters refer to like items in the following figures, and thus, once an item is defined in one figure, it need not be further defined and explained in subsequent figures.
The terms "first," "second," "third," and the like are used solely to distinguish one from another and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should also be noted that, unless otherwise explicitly specified or limited, the terms "disposed," "mounted," "connected," and "connected" are to be construed broadly and may, for example, be fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; the two elements can be directly connected or indirectly connected through an intermediate medium, and the two elements can be communicated with each other, so that the specific meaning of the terms in the invention can be understood by those skilled in the art.
In conjunction with FIG. 1:
a system for preparing high-purity magnesium oxide from magnesium chloride solution comprises a magnesium chloride solution tank 1, a high-pressure pump 2, a concentration washing tower 3, a spraying high-pressure pump 4, a hot blast stove 5, a spray drying tower 6, a cyclone powder collector 7, a dynamic calcining furnace 8, a finished product cyclone powder collector 9, a finished product tank 10, a primary absorption tower 11, a primary circulating absorption pump 12, a primary cooler 13, a secondary absorption tower 14, a secondary circulating pump 15, a secondary cooler 16, a tertiary absorption tower 17, a tertiary circulating pump 18, a tertiary cooler 19, a high-pressure induced draft fan 20, an alkali liquor washing tank 21 and a circulating washing pump 22, wherein the high-pressure pump 2 is connected to a pipeline between an outlet of the magnesium chloride solution tank 1 and an inlet of the concentration washing tower 3, the spraying high-pressure pump 4 is connected to a pipeline between an inlet of the spray drying tower 6 and an outlet of the concentration washing tower 3, an outlet of the spray drying tower 6 and an inlet of the cyclone powder collector 7 are mutually, the outlet of the cyclone powder collector 7 is communicated with the inlet of the concentration washing tower 3 through a pipeline, the air outlet of the hot blast stove 5 is respectively communicated with the inlets of the spray drying tower 6, the cyclone powder collector 7 and the dynamic calcining furnace 8 through pipelines, the outlet of the dynamic calcining furnace 8 is connected with the inlet of the finished product cyclone powder collector 9, one outlet of the finished product cyclone powder collector 9 is connected with the inlet of the spray drying tower 6 through a pipeline, the other outlet of the finished product cyclone powder collector 9 is communicated with the finished product charging bucket 10 through a pipeline, the magnesium chloride solution tank 1, the high-pressure pump 2, the concentration washing tower 3, the spray high-pressure pump 4, the hot blast stove 5, the spray drying tower 6, the cyclone powder collector 7, the dynamic calcining furnace 8, the finished product cyclone powder collector 9 and the finished product charging bucket 10 form a production system, and the primary absorption tower 11, the primary circulating absorption pump 12, the primary cooler 13, the secondary absorption, The absorption system consists of a secondary circulating pump 15, a secondary cooler 16, a tertiary absorption tower 17, a tertiary circulating pump 18, a tertiary cooler 19, a high-pressure induced draft fan 20, an alkali liquor washing tank 21 and a circulating washing pump 22.
In this embodiment, pass through the pipe connection in the export of concentrated scrubbing tower 3 on absorption system, absorption system is including the one-level absorption tower 11, second grade absorption tower 14, the tertiary absorption tower 17 that communicate in proper order, there are one-level cooler 13, second grade cooler 16, tertiary cooler 19 in the export of one-level absorption tower 11, second grade absorption tower 14, tertiary absorption tower 17 respectively pipe connection, there is the concentrated hydrochloric acid storage tank in the export of one-level cooler 13, second grade cooler 16, tertiary cooler 19 respectively pipe connection one-level absorption tower 11, second grade absorption tower 14, tertiary absorption tower 17, there is the concentrated hydrochloric acid storage tank in the export of one-level cooler 13, there is high pressure draught fan 20 in the export of tertiary absorption tower 17 through the pipe connection.
In this embodiment, the export of high pressure draught fan 20 has alkali lye washing tank 21 through the pipe connection, communicate respectively on the export of alkali lye washing tank 21 and have collection box and circulation scrubbing pump 22, the export of circulation scrubbing pump 22 is linked together with alkali lye washing tank 21.
In this embodiment, the outlets of the spray drying tower 6, the cyclone powder collector 7 and the finished product cyclone powder collector 9 are all provided with valves.
A use method of a system for preparing high-purity magnesium oxide from magnesium chloride solution comprises the following steps:
s1: feeding the refined solution with the magnesium chloride content of 35% into a magnesium chloride solution tank 1;
s2: starting the high-pressure draught fan 20, adjusting an air valve, starting the natural gas burner, controlling the gas quantity of the natural gas burner at 46 m/h, heating the hot blast stove 5, simultaneously starting a circulating pump of the hydrochloric acid absorption system and the concentration washing tower 3, starting the spraying high-pressure pump 4 to control the high-pressure flow when the outlet temperature of the dynamic calcining furnace 8 reaches about 400 ℃, gradually raising the temperature of the system, and when the outlet temperature of the dynamic calcining furnace 8 reaches about 520 ℃, enabling the system to enter a normal working state.
S3: and (3) carrying out high-pressure train year on the high-pressure pump 2 through regulating the output flow of the high-pressure pump by a valve, carrying out high-pressure train year on the natural gas burner, carrying out high-pressure train year on the high-pressure train year, carrying out high.
S4: the high-pressure pump 5 inputs the magnesium chloride solution in the magnesium chloride solution tank 1 into the concentration washing tower 3, the concentrated and washed magnesium chloride solution is input into the spray drying tower 6 under the action of the spray high-pressure pump 4 and reacts to form magnesium chloride monohydrate powder and hydrogen chloride gas, the dried magnesium chloride monohydrate powder falls into the bottom of the spray drying tower 6 and is sent to the dynamic calcining furnace 8, the airflow carries a part of the magnesium chloride monohydrate powder into the cyclone powder collector 7, the magnesium chloride monohydrate powder is collected and then is sent to the dynamic calcining furnace 8, the magnesium chloride monohydrate powder calcined in the dynamic calcining furnace 8 generates magnesium oxide and hydrogen chloride gas, the gas calcined under the action of the system air pressure carries magnesium oxide and enters the finished product cyclone powder collector 9, and the magnesium oxide powder falls into the finished product charging tank 10 after collection.
S5: the hydrogen chloride gas generated in the dynamic calciner 8 in the step S4 is returned to the spray drying tower 6 through a pipeline, and then returned to the concentration washing tower 3 through a pipeline of the cyclone powder collector 7, and discharged into the absorption system together with the hydrogen chloride gas in the concentration washing tower 3 through a pipeline.
S6: the hydrogen chloride gas in step S5 is sent to the primary absorption tower 11, the secondary absorption tower 14, and the tertiary absorption tower 17 in sequence through pipelines to be absorbed, cooled by the primary cooler 13, the secondary cooler 16, and the tertiary cooler 19, and finally input to the hydrochloric acid storage tank.
S7: in operation S6, the hydrogen chloride gas that has not been absorbed by the tertiary absorption tower 17 is pumped into the lye washing tank 21 by the high-pressure induced draft fan 20, and is repeatedly absorbed by the circulating wash pump 22.
The relevant reaction formula for this example is:
MgCl2·H2O →MgO+2HCl；
2HCl +Ga(OH)2 →GaCl2 + 2H2O。
the above embodiments are not intended to limit the shape, material, structure, etc. of the present invention in any way, and any simple modification, equivalent change and modification made to the above embodiments according to the technical spirit of the present invention are within the scope of the technical solution of the present invention.
Claims (7)
1. A system for preparing high-purity magnesium oxide from magnesium chloride solution is characterized in that: the device comprises a magnesium chloride solution tank, a high-pressure pump, a concentration washing tower, a spraying high-pressure pump, a hot blast stove, a spray drying tower, a cyclone powder collector, a dynamic calcining furnace, a finished product cyclone powder collector, a finished product tank, a primary absorption tower, a primary circulation absorption pump, a primary cooler, a secondary absorption tower, a secondary circulation pump, a secondary cooler, a tertiary absorption tower, a tertiary circulation pump, a tertiary cooler, a high-pressure induced draft fan, an alkali liquor washing tank and a circulation washing pump, wherein the high-pressure pump is connected to a pipeline between an outlet of the magnesium chloride solution tank and an inlet of the concentration washing tower, the spraying high-pressure pump is connected to a pipeline between the inlet of the spray drying tower and an outlet of the concentration washing tower, an outlet of the spray drying tower is communicated with the inlet of the cyclone powder collector through a pipeline, an outlet of the hot blast stove is respectively communicated with the spray drying tower, a spray drying tower and a, The inlet of the cyclone powder collector and the inlet of the dynamic calcining furnace are mutually communicated through a pipeline, the outlet of the dynamic calcining furnace is connected to the inlet of the finished product cyclone powder collector, one outlet of the finished product cyclone powder collector is connected to the inlet of the spray drying tower through a pipeline, the other outlet of the finished product cyclone powder collector is communicated with the finished product material tank through a pipeline, the magnesium chloride solution tank, the high-pressure pump, the concentration washing tower, the spray high-pressure pump, the hot blast stove, the spray drying tower, the cyclone powder collector, the dynamic calcining furnace, the finished product cyclone powder collector and the finished product material tank form a production system, and the absorption system consists of the primary absorption tower, the primary circulating absorption pump, the primary cooler, the secondary absorption tower, the secondary circulating pump, the secondary cooler, the tertiary absorption tower, the tertiary circulating pump, the tertiary cooler, the high-pressure induced.
2. The system for preparing high-purity magnesium oxide from magnesium chloride solution according to claim 1, wherein the outlet of the concentration washing tower is connected to an absorption system through a pipeline, the absorption system comprises a first-stage absorption tower, a second-stage absorption tower and a third-stage absorption tower which are sequentially communicated, the outlets of the first-stage absorption tower, the second-stage absorption tower and the third-stage absorption tower are respectively connected to a first-stage cooler, a second-stage cooler and a third-stage cooler through pipelines, the outlets of the first-stage cooler, the second-stage cooler and the third-stage cooler are respectively communicated to the first-stage absorption tower, the second-stage absorption tower and the third-stage absorption tower through pipelines, the outlet of the first-stage cooler is further connected to a concentrated hydrochloric acid storage tank through a pipeline, and the outlet of the third-stage absorption.
3. The system for preparing high-purity magnesium oxide from magnesium chloride solution according to claim 2, wherein the outlet of the high-pressure induced draft fan is connected with a lye washing tank through a pipeline, the outlet of the lye washing tank is respectively communicated with a recovery tank and a circulating washing pump, and the outlet of the circulating washing pump is communicated with the lye washing tank.
4. The use method of the system for preparing high-purity magnesium oxide from the magnesium chloride solution is characterized by comprising the following steps:
s1: pumping the magnesium chloride solution in the magnesium chloride solution pipe into a concentration washing tower through a high-pressure pump; concentrating in a concentrating washing tower and pumping into a spray drying tower by a spray high-pressure pump; meanwhile, the hot blast stove is opened, the dynamic calcining furnace is heated, the concentrated magnesium chloride solution in the spray drying tower reacts to obtain magnesium chloride dihydrate powder, and the magnesium chloride dihydrate powder is separated in a dry mode and a wet mode, then is sent into a cyclone powder collecting device and then is sent into the dynamic calcining furnace; calcining the magnesium chloride dihydrate in a dynamic calcining furnace to generate magnesium chloride and hydrogen chloride gas, collecting the magnesium chloride and the hydrogen chloride gas by a finished product cyclone powder collector, and finally sending the magnesium chloride and the hydrogen chloride gas into a finished product material pipe;
s2: when the step S1 is operated, the trace magnesium chloride solution generated by the cyclone powder collector is conveyed to the concentration washing tower again through the pipeline for standby, and the magnesium chloride dihydrate powder in the finished product cyclone powder collector is conveyed to the dynamic calcining furnace again through the pipeline for re-reaction;
s3: when the step S1 is operated, hydrogen chloride gas generated when the concentration washing tower works is sequentially conveyed to the first-stage absorption tower, the second-stage absorption tower and the third-stage absorption tower through pipelines to be absorbed, and is cooled by the first-stage cooler, the second-stage cooler and the third-stage cooler and finally input into the hydrochloric acid storage tank;
and S4, pumping the hydrogen chloride gas which is not absorbed by the three-stage absorption tower into an alkali liquor washing tank through a high-pressure induced draft fan and repeatedly absorbing the hydrogen chloride gas through a circulating washing pump when the operation is performed in the step S3.
5. Use of a system for the preparation of high purity magnesium oxide from magnesium chloride solution according to claim 4, wherein said high pressure pump is valved to deliver an output flow rate of 0.50 to 0.55m plantation.
6. The use method of the system for preparing high-purity magnesium oxide from magnesium chloride solution according to claim 4, wherein the temperature of the outlet of the hot blast stove is stabilized at 860 ℃, when the temperature of the outlet of the dynamic calcining tower reaches about 400 ℃, the spraying high-pressure pump is started to control the high-pressure flow, so that the temperature of the system is gradually increased, and when the temperature of the outlet of the dynamic calcining furnace reaches 500-530 ℃, the system enters a normal working state.
7. The use of the system for preparing high purity magnesium oxide from magnesium chloride solution according to claim 4, wherein the concentration of the magnesium chloride solution is 30% -40%.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113998723A (en) * | 2021-12-16 | 2022-02-01 | 昊华宇航化工有限责任公司 | Production device and method of polyaluminum chloride |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1009337A (en) * | 1961-10-26 | 1965-11-10 | Zentrale Forschungsstelle Fuer | Magnesium oxide preparation |
| CN1830787A (en) * | 2006-03-21 | 2006-09-13 | 中国科学院青海盐湖研究所 | Method of preparing high purity magnesium oxide by closed pyrolysis magnesium chloride hydrate |
| CN101007643A (en) * | 2006-12-21 | 2007-08-01 | 青海中信国安科技发展有限公司 | Process and apparatus for preparing magnesium oxide and hydrogen chloride mixed gas by two-stage dynamic calcining of magnesium chloride |
| US20070219081A1 (en) * | 2006-03-15 | 2007-09-20 | Council Of Scientific & Industrial Research | Process for the preparation of magnesia (MgO) |
| CN104773744A (en) * | 2014-01-15 | 2015-07-15 | 中国科学院过程工程研究所 | Method for preparing high purity magnesium oxide from old brine |
| CN105197968A (en) * | 2015-09-15 | 2015-12-30 | 中国科学院过程工程研究所 | Method and device for producing high-purity magnesium oxide and co-producing industrial concentrated hydrochloric acid through partially hydrated magnesium chloride fluidization pyrolysis |
| CN107986304A (en) * | 2017-12-27 | 2018-05-04 | 鞍钢实业微细铝粉有限公司 | A kind of preparation process of nano magnesia |
-
2020
- 2020-07-30 CN CN202010752709.2A patent/CN111807390A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1009337A (en) * | 1961-10-26 | 1965-11-10 | Zentrale Forschungsstelle Fuer | Magnesium oxide preparation |
| US20070219081A1 (en) * | 2006-03-15 | 2007-09-20 | Council Of Scientific & Industrial Research | Process for the preparation of magnesia (MgO) |
| CN1830787A (en) * | 2006-03-21 | 2006-09-13 | 中国科学院青海盐湖研究所 | Method of preparing high purity magnesium oxide by closed pyrolysis magnesium chloride hydrate |
| CN101007643A (en) * | 2006-12-21 | 2007-08-01 | 青海中信国安科技发展有限公司 | Process and apparatus for preparing magnesium oxide and hydrogen chloride mixed gas by two-stage dynamic calcining of magnesium chloride |
| CN104773744A (en) * | 2014-01-15 | 2015-07-15 | 中国科学院过程工程研究所 | Method for preparing high purity magnesium oxide from old brine |
| CN105197968A (en) * | 2015-09-15 | 2015-12-30 | 中国科学院过程工程研究所 | Method and device for producing high-purity magnesium oxide and co-producing industrial concentrated hydrochloric acid through partially hydrated magnesium chloride fluidization pyrolysis |
| CN107986304A (en) * | 2017-12-27 | 2018-05-04 | 鞍钢实业微细铝粉有限公司 | A kind of preparation process of nano magnesia |
Non-Patent Citations (1)
| Title |
|---|
| 闫岩等: "利用老卤生产高纯氧化镁技术研究进展", 《化工进展》 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113998723A (en) * | 2021-12-16 | 2022-02-01 | 昊华宇航化工有限责任公司 | Production device and method of polyaluminum chloride |
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