CN113683103B - Light magnesium carbonate production device and method based on resource utilization - Google Patents
Light magnesium carbonate production device and method based on resource utilization Download PDFInfo
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- CN113683103B CN113683103B CN202111160096.4A CN202111160096A CN113683103B CN 113683103 B CN113683103 B CN 113683103B CN 202111160096 A CN202111160096 A CN 202111160096A CN 113683103 B CN113683103 B CN 113683103B
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- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 title claims abstract description 59
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 29
- 238000000034 method Methods 0.000 title claims abstract description 16
- 238000000197 pyrolysis Methods 0.000 claims abstract description 133
- 238000003763 carbonization Methods 0.000 claims abstract description 127
- 230000029087 digestion Effects 0.000 claims abstract description 122
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims abstract description 58
- 238000006243 chemical reaction Methods 0.000 claims abstract description 41
- 239000007789 gas Substances 0.000 claims abstract description 39
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims abstract description 37
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims abstract description 33
- 229910052749 magnesium Inorganic materials 0.000 claims abstract description 33
- 239000011777 magnesium Substances 0.000 claims abstract description 33
- 239000007788 liquid Substances 0.000 claims abstract description 31
- 229910000019 calcium carbonate Inorganic materials 0.000 claims abstract description 29
- 239000000395 magnesium oxide Substances 0.000 claims abstract description 29
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims abstract description 23
- 238000010438 heat treatment Methods 0.000 claims abstract description 11
- 239000007787 solid Substances 0.000 claims abstract description 8
- 239000002994 raw material Substances 0.000 claims abstract description 7
- 239000006227 byproduct Substances 0.000 claims abstract description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical group O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 125
- 239000002002 slurry Substances 0.000 claims description 51
- 238000005406 washing Methods 0.000 claims description 40
- 239000012452 mother liquor Substances 0.000 claims description 39
- 239000012065 filter cake Substances 0.000 claims description 38
- 239000000843 powder Substances 0.000 claims description 26
- 230000035484 reaction time Effects 0.000 claims description 24
- 238000001035 drying Methods 0.000 claims description 23
- 238000001704 evaporation Methods 0.000 claims description 22
- 230000008020 evaporation Effects 0.000 claims description 22
- 239000000463 material Substances 0.000 claims description 17
- 238000000926 separation method Methods 0.000 claims description 17
- 238000000227 grinding Methods 0.000 claims description 14
- 239000000706 filtrate Substances 0.000 claims description 11
- QWDJLDTYWNBUKE-UHFFFAOYSA-L magnesium bicarbonate Chemical compound [Mg+2].OC([O-])=O.OC([O-])=O QWDJLDTYWNBUKE-UHFFFAOYSA-L 0.000 claims description 11
- 229910000022 magnesium bicarbonate Inorganic materials 0.000 claims description 11
- 239000002370 magnesium bicarbonate Substances 0.000 claims description 11
- 235000014824 magnesium bicarbonate Nutrition 0.000 claims description 11
- 230000014759 maintenance of location Effects 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 6
- 238000004806 packaging method and process Methods 0.000 claims description 6
- 230000001079 digestive effect Effects 0.000 claims description 5
- 235000011389 fruit/vegetable juice Nutrition 0.000 claims description 5
- 239000004615 ingredient Substances 0.000 claims description 5
- 239000000047 product Substances 0.000 claims description 5
- 239000001095 magnesium carbonate Substances 0.000 claims description 4
- 229910000021 magnesium carbonate Inorganic materials 0.000 claims description 4
- 230000005540 biological transmission Effects 0.000 claims description 3
- 239000012495 reaction gas Substances 0.000 claims description 3
- HHSPVTKDOHQBKF-UHFFFAOYSA-J calcium;magnesium;dicarbonate Chemical compound [Mg+2].[Ca+2].[O-]C([O-])=O.[O-]C([O-])=O HHSPVTKDOHQBKF-UHFFFAOYSA-J 0.000 claims description 2
- 238000002156 mixing Methods 0.000 abstract description 12
- 238000003756 stirring Methods 0.000 abstract description 6
- 230000000694 effects Effects 0.000 abstract description 4
- 239000000654 additive Substances 0.000 abstract description 3
- 230000000996 additive effect Effects 0.000 abstract description 3
- 238000004134 energy conservation Methods 0.000 abstract description 3
- 238000000605 extraction Methods 0.000 abstract description 3
- 239000002861 polymer material Substances 0.000 abstract description 3
- 239000000126 substance Substances 0.000 abstract description 3
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 125000004122 cyclic group Chemical group 0.000 abstract 1
- 239000012530 fluid Substances 0.000 description 18
- 238000005265 energy consumption Methods 0.000 description 6
- 238000009826 distribution Methods 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000010168 coupling process Methods 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000009792 diffusion process Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000005381 potential energy Methods 0.000 description 2
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical group [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
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000002075 main ingredient Substances 0.000 description 1
- 238000010907 mechanical stirring Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 231100000241 scar Toxicity 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F5/00—Compounds of magnesium
- C01F5/24—Magnesium carbonates
-
- 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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/141—Feedstock
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Inorganic Chemistry (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Abstract
The invention relates to a light magnesium carbonate production device and a method based on resource utilization, belonging to the technical field of chemical industry, wherein the device comprises a digestion tank, a carbonization tank, a pyrolysis tank, a flash tank, a horizontal double-drum centrifuge, a hollow blade dryer, an air flow mill and an air flow classifier; the raw material is low-grade magnesium oxide, and through two-stage serial continuous digestion, pyrolysis and pyrolysis reactions, a novel jet stirrer is adopted, and high-speed jet mixing and stirring are adopted, so that heat transfer and mass transfer are enhanced, and the gas, liquid and solid mixing and stirring effects are improved; low-pressure steam generated in the processes of digestion, carbonization and pyrolysis is subjected to MVR to generate secondary steam serving as an auxiliary heating source, so that comprehensive energy conservation is realized by 36%; the extraction rate of magnesium oxide is more than 90%, the content of magnesium oxide in the light magnesium carbonate is more than 46.5%, and the byproduct superfine magnesium-containing calcium carbonate is an additive of a high polymer material. The invention has simple process flow, continuous operation, high automation degree, cyclic utilization of resources and environmental protection, and realizes reasonable utilization of low-grade magnesium oxide resources.
Description
Technical Field
The invention belongs to the field of chemical equipment, and particularly relates to a light magnesium carbonate production device and method based on resource utilization.
Background
The light magnesium carbonate is generally produced by digestion, carbonization and pyrolysis of magnesium oxide. Digestion reaction, carbonization reaction and pyrolysis reaction generally adopt a kettle type reactor and a mechanical stirring or tubular type reactor. The preparation method has the defects that the kettle type reactor transfers heat through a jacket or an inner coil, and the heat exchange efficiency is low; the heat loss in the heat exchange process of the water vapor and the heavy magnesium water is more. Heavy magnesium water is easy to scar on the surface of the pyrolyzer in the pyrolysis process, so that the heat transfer efficiency of the pyrolyzer is reduced, the heat exchange efficiency of the pyrolyzer is low, the operation period is short, continuous production is not realized, and the system cannot stably run for a long period. In the method, the energy consumption in the digestion reaction, carbonization reaction and pyrolysis reaction stages is large, and the energy consumption accounts for more than 80% of the energy consumption of the whole process, and the increase of the energy consumption leads to the rise of cost, which is not beneficial to industrial production.
The art is eager to find a low-energy-consumption process for preparing light magnesium carbonate, which can overcome the technical problems.
Disclosure of Invention
Aiming at the engineering problems and market demands, the invention provides a light magnesium carbonate production device and a light magnesium carbonate production method for realizing reasonable utilization of low-grade magnesium oxide resources in light burned magnesium, which have the advantages of simple process flow, continuous operation, high automation degree, resource recycling and environmental friendliness, and are used for overcoming the problems in the prior art, and simultaneously recovering CO generated by pyrolysis reaction 2 And the MVR technology is utilized to recycle heat generated in carbonization reaction, pyrolysis reaction and drying process, so that the energy consumption is greatly reduced.
In order to achieve the above purpose, the present invention adopts the following technical scheme:
the light magnesium carbonate production device based on resource utilization comprises a digestion tank I, a digestion tank II, a carbonization tank I, a carbonization tank II and a flash tank which are sequentially connected, wherein the flash tank comprises a flash tank I and a flash tank II, and a pyrolysis tank I and a pyrolysis tank II are arranged between the flash tanks I, II; the flash tanks I, II are respectively connected with centrifuges I, II; the digestion tank I, II is used for performing digestion reaction on materials; the carbonization tank I, II is used for performing carbonization reaction on the digested slurry; the flash tank I is used for flashing carbonized slurry; the centrifugal machine I is used for carrying out solid-liquid separation on the carbonized slurry after flash evaporation; the pyrolysis tank I, II is used for carrying out pyrolysis reaction on the magnesium bicarbonate filtrate separated from the solid and the liquid; the flash tank II is used for flashing pyrolysis slurry; the centrifugal machine II is used for carrying out solid-liquid separation on the pyrolysis slurry subjected to flash evaporation to obtain a light magnesium carbonate filter cake;
wherein the digestion tank I, the digestion tank II, the carbonization tank I, the carbonization tank II, the pyrolysis tank I and the pyrolysis tank IThe stirrers arranged in the I are jet stirrers; CO of the carbonization tank I 2 The gas inlet is connected with CO of the carbonization tank II and the pyrolysis tank I, II 2 A gas outlet, the carbonization tank I discharges CO in the carbonization tank II and the pyrolysis tank I, II 2 The gas is reaction gas;
the device also comprises a compressor, wherein the input end of the compressor is connected with a flash tank I, II, a dryer I, II, and the output end of the compressor is connected with a digestion tank I, II, so that the steam generated by the flash tank I, II and the steam generated by the dryer I, II for drying the filter cake are collected, then boosted and heated to secondary steam, and the secondary steam is used as a heat source of the digestion tank I, II.
Further, the device also comprises a dryer I, II, an air flow mill I, II, an air flow classifier I, II, a steam condensate water tank, and a mother liquor and washing water tank; the dryer I, the air flow mill I and the air flow classifier I are used for drying, grinding and classifying the filter cakes separated from the solid and liquid to obtain byproducts; the dryer II, the air flow mill II and the air flow classifier II are used for drying, grinding and classifying the light magnesium carbonate filter cake obtained by solid-liquid separation to obtain a product light magnesium oxide; the carbonization tank I, II, the pyrolysis tank I, II and the heat source of the dryer I, II are steam;
a cooler is further arranged on the gas discharge pipeline of the carbonization tank I and is used for cooling CO discharged by the carbonization tank I 2 A gas; the pyrolysis tank I, II takes air separated by an air classifier I, II and an air mill I, II as an auxiliary heat source, and an air heater is arranged on an air transmission pipeline;
the input end of the steam condensate water tank is connected with the dryer I, II, the output end of the steam condensate water tank is connected with the centrifuge I, II and the digestion tank I, and the steam condensate water is used for collecting steam condensate water formed in the drying process after raw steam is introduced into the dryer I, II, and the steam condensate water is collected into the steam condensate water tank after being heated by the air heater to serve as washing water of the centrifuge I, II and batching water of the digestion tank I;
the input end of the mother liquor and the washing water tank is connected with the centrifugal machine II, the output end of the mother liquor and the washing water tank is connected with the digestion tank I, and the mother liquor and the washing water after being centrifuged by the centrifugal machine II are collected and cooled by the coolerCO discharged from the carbonization tank I 2 The gas enters a digestion tank I and is used as the ingredient water of the digestion tank I.
The invention also provides a light magnesium carbonate production method based on resource utilization, which comprises the following steps:
(1) Raw materials of magnesium oxide, mother liquor, washing water and steam condensate water enter a digestion tank I, and secondary steam is directly heated for digestion reaction;
(2) Feeding the digestion slurry in the digestion tank I into the digestion tank II, and directly heating by using secondary water vapor to continue digestion reaction;
(3) Feeding the digestive juice in the digestion tank II into the carbonization tank I, and sucking CO discharged by the carbonization tank II 2 CO discharged by gas, pyrolysis tank I and pyrolysis tank II 2 The gas is directly heated by raw steam to carry out carbonization reaction;
(4) Introducing carbonized slurry in the carbonization tank I into the carbonization tank II, and simultaneously introducing fresh CO 2 Directly heating the gas by using raw steam to continue carbonization reaction;
(5) Feeding carbonized slurry in a carbonization tank II into a flash tank I, and flashing out low-pressure water vapor;
(6) Feeding the carbonized slurry subjected to flash evaporation in the flash evaporation tank I into a centrifugal machine I for centrifugal separation to separate a magnesium-containing calcium carbonate filter cake and magnesium bicarbonate filtrate;
(7) Feeding the magnesium bicarbonate filtrate separated by the centrifugal machine I into a pyrolysis tank I, and simultaneously carrying out pyrolysis reaction on the sucked hot air and raw steam;
(8) Feeding the pyrolysis slurry in the pyrolysis tank I into the pyrolysis tank II, and continuously carrying out pyrolysis reaction by using hot air and raw steam which are sucked in at the same time;
(9) Feeding pyrolysis slurry in a pyrolysis tank II into a flash tank II, and flashing out low-pressure water vapor;
(10) Feeding the pyrolysis slurry subjected to flash evaporation in the flash tank II into a centrifugal machine II for centrifugal separation, feeding separated mother liquor and washing water into a mother liquor and a washing water tank, and cooling CO discharged by a carbonization tank I through a carbonization tank I cooler 2 Then enters a digestion tank I; and (3) centrifugally separating out a light magnesium carbonate filter cake by a centrifugal machine II.
Further, the raw magnesia in the step (1) is low-quality magnesia which is obtained by classifying light-burned magnesia, wherein the mass fraction of the magnesia is 60% -65%, the balance is calcium oxide, and the mass ratio of particles with the particle diameter smaller than 0.075mm in the low-quality magnesia is 95%; the raw steam is back pressure steam of 0.4MPa and 230 ℃ of a self-contained power plant; the raw steam mainly provides heat sources for carbonization reaction, pyrolysis reaction, a dryer I and a dryer II, steam condensate water is used as auxiliary ingredient water, and mother liquor and washing water are used as main ingredient water; the heat source of the digestion reaction is provided by vapor generated by a flash tank I, a flash tank II, a dryer I and a dryer II through Mechanical Vapor Recompression (MVR), namely secondary vapor of pressure boosting and temperature rising of a compressor; the secondary steam temperature is 221 ℃, and the pressure is 0.15 MPa.
Further, the fresh CO 2 The gas is CO recovered from light burned magnesium oxide 2 Mixed gas of CO 2 The volume fraction of the gas is 30% -35%.
Further, in the step (1), the digestion temperature of the digestion tank I is 80-85 ℃, the pressure is 0.35MPa, the digestion reaction time is 0.5-1 h, and the solid-liquid mass ratio is 1: (27-30), sucking secondary water vapor through a jet stirrer to directly heat digestion slurry; the digestion temperature of the digestion tank II in the step (2) is 85-90 ℃, the pressure is 0.3MPa, and the digestion reaction time is 0.5-1 h; the secondary steam is sucked in by a jet stirrer to directly heat the digestive juice.
Further, the carbonization temperature of the carbonization tank I in the step (3) is 90-93 ℃, the pressure is 0.275MPa, and the carbonization reaction time is 1-1.5 h; CO discharged from raw steam, carbonization tank II and pyrolysis tank I, II 2 Sucking into a carbonization tank I through a jet stirrer; the carbonization temperature of the carbonization tank II in the step (4) is 93-96 ℃, the pressure is 0.25MPa, the carbonization reaction time is 1-1.5 h, and the raw steam and fresh CO are generated 2 Sucking into carbonization tank II via jet stirrer.
Further, in the steps (5) and (9), the flash tank I, II is operated adiabatically at a flash temperature of 80 ℃, and the flashed vapor enters the compressor.
Further, in the step (7): the pyrolysis temperature of the pyrolysis tank I is 105-110 ℃, the pressure is 0.25MPa, and the pyrolysis reaction time is 1-1.25 h; raw steam and hot air are sucked into the pyrolysis tank I through the jet stirrer; in the step (8): the pyrolysis temperature of the pyrolysis tank II is 110-115 ℃, the pressure is 0.20MPa, and the pyrolysis reaction time is 1-1.25 h; raw steam and hot air are sucked into the pyrolysis tank II through the jet stirrer.
Further, in the steps (6) and (10), the centrifugal machines I, II are horizontal double-drum centrifugal machines, in particular horizontal double-drum spiral discharge centrifugal machines, the outer drum of the centrifugal machine I, II is 2400rpm, the inner drum is 2410rpm, the retention time of materials in the centrifugal machines is 5min, and the temperatures of magnesium calcium carbonate filter cakes and magnesium carbonate filter cakes are 70 ℃; the mother liquor and the washing water separated by the centrifugal machine II are fed into a mother liquor and a washing water tank, and the mother liquor and the washing water cool CO discharged by the carbonization tank I 2 And then enters a digestion tank I.
Further, the step (6) further includes: feeding the magnesium-containing calcium carbonate filter cake into a dryer I through a spiral feeder to be dried by using raw steam; feeding the dried magnesium-containing calcium carbonate into an air flow mill I for grinding; the ground magnesium-containing calcium carbonate powder is fed into an air classifier I for classification, and the classified magnesium-containing calcium carbonate powder is finished and packaged to leave the factory; the step (10) further comprises: feeding the light magnesium carbonate filter cake into a dryer II through a spiral feeder, and drying by using raw steam; feeding the dried light magnesium carbonate powder into an air flow mill II for grinding; and (3) feeding the ground light magnesium carbonate powder into an air classifier II for classification, and packaging to leave a factory after classification to obtain the finished light magnesium carbonate powder.
Further, in the steps (6) and (10), the dryer I, II is a hollow blade dryer, the drying heat source is steam, the steam is respectively introduced into the jacket and the hollow blade of the hollow blade dryer I, II, and the condensed water of the steam is collected in the steam condensate water tank after the air is heated; the water vapor generated by drying the filter cake is heated and boosted by a compressor to be used as secondary water vapor; the temperature in the dryer I, II is 135-140 ℃, the pressure is 0.313-0.361 MPa, and the material retention time is 0.75-1.5 h; the temperature of the discharged water vapor is 135-140 ℃, and the pressure is 0.313-0.361 MPa; the temperature of the steam condensate discharged by the jacket and the hollow blade of the dryer I, II is 135-140 ℃, and the temperature of the dry material discharged by the hollow blade dryer I, II is 135-140 ℃.
Compared with the prior art, the light magnesium carbonate production device and method based on resource utilization have the beneficial effects that:
1. the raw material magnesium oxide is low-grade magnesium oxide with the mass content of 60-65 percent; the raw steam is back pressure steam of a self-contained power plant, and the secondary steam is MVR-passing steam generated in the processes of digestion reaction, carbonization reaction, pyrolysis reaction and drying; CO 2 The light burned magnesium and pyrolysis are recycled, and the batching water is steam condensate water, mother liquor and washing water; the air needed by pyrolysis is heated by the steam condensate water which is dried and separated; resources are effectively utilized, and the environment is protected.
2. The two-stage serial continuous digestion, pyrolysis and pyrolysis kettles all adopt novel jet mixers, high-speed jet mixing and stirring are adopted, heat transfer and mass transfer are enhanced, the mixing and stirring effects of gas, liquid and solid are improved, and the production efficiency is improved;
3. low-pressure steam generated in the processes of digestion reaction, carbonization reaction, pyrolysis reaction and drying generates secondary steam through MVR, and the secondary steam at the temperature of 0.15MPa and 221 ℃ is taken as an auxiliary heating source, so that the comprehensive energy conservation is realized by 36%;
4. the extraction rate of magnesium oxide is more than 90%, the content of magnesium oxide in light magnesium carbonate is more than 46.5%, the magnesium oxide is higher than the standard of GB/T27814-2011 superior products, and the byproduct superfine magnesium-containing calcium carbonate is an additive of high polymer materials.
Drawings
FIG. 1 is a schematic diagram of a light magnesium carbonate production device based on resource utilization;
FIG. 2 is a flow chart of raw steam of the production device according to the invention;
FIG. 3 is a flow chart of steam condensate, carbon dioxide, mother liquor and wash water of the production device according to the invention;
FIG. 4 is a flow chart of secondary steam and hot air in the production device according to the present invention;
reference numerals: 1. digestion tank I;1-1, a jet stirrer; 1-2, a power fluid pump; 2. a digestion tank II;2-1, a jet stirrer; 2-2, a power fluid pump; 3. a carbonization tank I;3-1, jet mixer; 3-2, a power fluid pump; 3-3, a cooler; 4. a carbonization tank II;4-1, a jet stirrer; 4-2, a power fluid pump; 5. a flash tank I; 6. a horizontal double-drum centrifuge I; 7. a hollow blade dryer I; 8. air flow mill I; 9. an air classifier I; 10. a pyrolysis tank I;10-1, jet mixer; 10-2, a power fluid pump; 11. a pyrolysis tank II;11-1, jet stirrer; 11-2, a power fluid pump; 12. a flash tank II; 13. a horizontal double-drum centrifuge II; 14. a hollow blade dryer II; 15. air flow mill II; 16. an air classifier II;17 compressors; 18 mother liquor and a washing water tank; 19. an air heater; 20. a blower; 21. and a steam condensate water tank.
Detailed Description
The present invention will be described in further detail with reference to the following examples in order to make the objects, technical solutions and advantages of the present invention more apparent. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.
Example 1
As shown in fig. 1 to 4, a light magnesium carbonate production device based on resource utilization comprises a digestion tank I1, a digestion tank II 2, a carbonization tank I3, a carbonization tank II 4 and a flash tank which are sequentially connected, wherein the flash tank comprises a flash tank I5 and a flash tank II 12, and a pyrolysis tank I10 and a pyrolysis tank II 11 are arranged between the flash tanks I, II; the flash tanks I, II are respectively connected with horizontal double-drum centrifuges I, II (6 and 13); the digestion tank I, II is used for performing digestion reaction on materials; the carbonization tank I, II is used for performing carbonization reaction on the digested slurry; the flash tank I is used for flashing carbonized slurry; the centrifugal machine I is used for carrying out solid-liquid separation on the carbonized slurry after flash evaporation; the pyrolysis tank I, II is used for carrying out pyrolysis reaction on the magnesium bicarbonate filtrate separated from the solid and the liquid; the flash tank II is used for flashing pyrolysis slurry; the centrifugal machine II is used for carrying out solid-liquid separation on the pyrolysis slurry subjected to flash evaporation; obtaining a light magnesium carbonate filter cake;
wherein, the agitators arranged in the digestion tank I, the digestion tank II, the carbonization tank I, the carbonization tank II, the pyrolysis tank I and the pyrolysis tank II are jet agitators; CO of the carbonization tank I 2 The gas inlet is connected with CO of the carbonization tank II and the pyrolysis tank I, II 2 A gas outlet, the carbonization tank I discharges CO in the carbonization tank II and the pyrolysis tank I, II 2 The gas is reaction gas;
the device further comprises a compressor 17, wherein the input end of the compressor is connected with a flash tank I, II, the dryer I, II is connected with a digestion tank I, II, and the output end of the compressor is connected with the digestion tank I, II, so that steam generated by the flash tank I, II and steam generated by drying a filter cake by the dryer I, II are collected and then are subjected to mechanical steam recompression (MVR), namely secondary steam formed by boosting and heating of the compressor is respectively introduced into the digestion tank I, II to serve as a heat source of the digestion tank I, II.
Wherein the device further comprises a hollow blade dryer I, II (7, 14), an air mill I, II (8, 15), an air classifier I, II (9, 16), a steam condensate water tank 21 and a mother liquor and wash water tank 18; the dryer I, the air flow mill I and the air flow classifier I are used for drying, grinding and classifying the filter cakes separated from the solid and liquid to obtain byproducts; the dryer II, the air flow mill II and the air flow classifier II are used for drying, grinding and classifying the light magnesium carbonate filter cake obtained by solid-liquid separation to obtain a product light magnesium oxide; the carbonization tank I, II, the pyrolysis tank I, II and the heat source of the dryer I, II are steam;
the gas discharge pipeline of the carbonization tank I is also provided with a cooler 3-3 which is used for cooling CO discharged by the carbonization tank I 2 A gas; the pyrolysis tank I, II takes air separated by an air classifier I, II and an air mill I, II as an auxiliary heat source, and an air heater 19 and a fan 20 are arranged on an air transmission pipeline;
the input end of the steam condensate water tank is connected with a dryer I, II, the output end of the steam condensate water tank is connected with a centrifuge I, II and a digestion tank I, and the steam condensate water is used for collecting steam condensate water formed in the drying process after raw steam is introduced into a jacket of a hollow blade dryer I, II and hollow blades, and is collected into the steam condensate water tank after air is heated by an air heater to serve as washing water of the centrifuge I, II and batching water of the digestion tank I;
the input end of the mother liquor and the washing water tank is connected with the centrifugal machine II, the output end of the mother liquor and the washing water tank is connected with the digestion tank I, the mother liquor and the washing water after being centrifuged by the centrifugal machine II are collected, and the mother liquor and the washing water are cooled by the cooler and are subjected to CO discharged by the carbonization tank I 2 The gas enters a digestion tank I and is used as the ingredient water of the digestion tank I.
Wherein, the digestion tank I, the digestion tank II, the carbonization tank I, the carbonization tank II, the pyrolysis tank I and a power fluid pump (1-2, 2-2, 3-2, 4-2, 10-2, 11-2) arranged outside the pyrolysis tank II, the digestion tank I, the digestion tank II, the carbonization tank I, the carbonization tank II, the pyrolysis tank I and jet agitators (1-1, 2-1, 3-1, 4-1, 10-1, 11-1) arranged in the pyrolysis tank II are composed of a plurality of jet devices and a coupling distributor, wherein the coupling distributor is composed of a mixed liquid inlet pipe, a mixed liquid distribution cavity, a gas suction pipe, a gas distribution cavity and the like; the jet device adopts a venturi jet principle and consists of a power fluid inlet, a guide ring, a power fluid nozzle, a gas suction inlet, a mixing cavity, a diffusion cavity and a mixed liquid outlet; and during operation, the circulating pump pumps cancel the mixed liquid in the dissolving tank, the mixed liquid is pumped into the mixed liquid distribution cavity through the mixed liquid inlet pipe after being boosted by the impeller, and the mixed liquid distributed through the distribution cavity enters into each ejector through the mixed liquid inlet of each ejector. The dynamic fluid passes through the nozzle to form high-speed fluid, at the moment, the kinetic energy of the fluid is maximum and the potential energy is minimum, negative pressure is generated at the gas suction inlet, then the gas is sucked, the sucked gas is rapidly expanded in the negative pressure area and is beaten into tiny bubbles by the dynamic fluid, and in the mixing cavity, the gas (water vapor, CO 2 Hot air), water and magnesium oxide powder are fully mixed, fluid is subjected to intensive mixing and stirring in a mixing zone, the fluid is accelerated to be discharged due to energy exchange, potential energy of the mixed fluid is increased to the maximum value through a diffusion cavity, the mixed fluid is emitted to the bottom of the tank in a tangential direction, and the mixing and stirring effect is further enhanced due to the dragging effect of the mixed fluid. The gas is sucked into the digestion tank by the jet mixing stirrer, and the gas-liquid mixing cavity of the jet mixing stirrer can be used forGenerating 300m/s high-speed jet flow, which is beneficial to the digestion reaction of water and raw material magnesia powder;
when the production device is started, the digestion tank I adopts process water as ingredient water, the digestion tank I, II adopts raw steam as starting steam (not shown in a starting pipeline diagram) until the whole production device operates normally, when secondary steam is insufficient, the raw steam also serves as an auxiliary heating source of the digestion tank I, II, all device equipment are connected through corresponding pipelines, and when the pipelines in the figures 1-4 intersect on the figure but do not intersect actually, the digestion tank is drawn according to the principle of vertical and horizontal continuous.
Example 2
The method for producing the light magnesium carbonate based on the recycling utilization based on the device of the embodiment 1 comprises the following steps:
(1) 2000kg/h (charging rate) of raw material low-quality magnesium oxide (magnesium oxide mass fraction 65%), mother liquor and washing water, 54045kg/h (charging rate) of heating steam condensate water are fed into a digestion tank I; the digestion temperature of the digestion tank I is 80 ℃, the pressure is 0.35MPa, the digestion reaction time is 1h, and the solid-liquid mass ratio is 1:30, secondary steam 221 ℃,0.15MPa,5000kg/h (feed rate) was sucked in through a jet stirrer to directly heat the digested slurry.
(2) Feeding the digestion slurry in the digestion tank I into a digestion tank II, wherein the digestion temperature of the digestion tank II is 85 ℃, the pressure is 0.3MPa, the digestion reaction time is 1h, the secondary water vapor is 221 ℃, and 0.15MPa and 1700kg/h of the digestion slurry are sucked through a jet stirrer to directly heat the digestion slurry.
(3) Feeding the digested slurry in the digestion tank II into the carbonization tank I, and sucking CO discharged from the carbonization tank II and the pyrolysis tank I, II 2 A gas; the carbonization temperature of the carbonization tank I is 90 ℃, the pressure is 0.275MPa, the carbonization reaction time is 1.5h, the raw steam is 230 ℃, the pressure is 0.4MPa, the charging rate is 760kg/h, and the CO discharged by the carbonization tank II and the pyrolysis tank I, II 2 Sucked into the carbonization tank I through a jet stirrer.
(4) Feeding carbonized slurry in a carbonization tank I into a carbonization tank II, wherein the carbonization temperature of the carbonization tank II is 93 ℃, the pressure is 0.25MPa, the carbonization reaction time is 1.5h, the raw steam is 1000kg/h, and the fresh CO is fresh 2 220kmol/h (rate of introduction, CO-containing recovered from light burned magnesia) 2 Gas, CO 2 35% by volume) was sucked into carbonization tank II via a jet stirrer.
(5) And (3) feeding carbonized slurry in the carbonization tank II into a flash tank I, flashing out low-pressure water vapor, wherein the temperature of the flash tank I is 80 ℃, carrying out adiabatic flash evaporation, and feeding the flashed vapor into a compressor.
(6) Feeding carbonized slurry subjected to flash evaporation in a flash evaporation tank I into a horizontal double-drum centrifuge I, and performing centrifugal separation to obtain a magnesium-containing calcium carbonate filter cake and magnesium bicarbonate filtrate; the outer rotary drum of the centrifuge is 2400rpm, the inner rotary drum is 2410rpm, the retention time of the materials in the centrifuge is 5min, and the temperature of the magnesium-containing calcium carbonate filter cake is 70 ℃;
wherein:
(6-1) feeding the magnesium-containing calcium carbonate filter cake into a hollow blade dryer I through a screw conveyor, and drying with 300kg/h of raw steam; the temperature in the hollow blade dryer I is 140 ℃, the pressure is 0.361MPa, and the material residence time is 1.5h; the temperature of the discharged water vapor is 140 ℃, the pressure is 0.361MPa, and the discharged water vapor enters a compressor; the temperature of the steam condensate water discharged by the jacket of the hollow blade dryer I is 140 ℃, and the temperature of the dried magnesium-containing calcium carbonate powder discharged by the hollow blade dryer I is 140 ℃;
(6-2) feeding the dried magnesium-containing calcium carbonate into an air flow mill I for grinding;
and (6-3) feeding the ground magnesium-containing calcium carbonate powder into an air classifier I for classification, and packaging to leave a factory after classification to obtain finished magnesium-containing calcium carbonate powder.
(7) Feeding the magnesium bicarbonate filtrate separated by the horizontal double-drum centrifuge I into a pyrolysis tank I, wherein the pyrolysis temperature of the pyrolysis tank I is 105 ℃, the pressure is 0.25MPa, and the pyrolysis reaction time is 1.25h; 2400kg/h of raw steam and hot air are sucked into the pyrolysis tank I through the jet stirrer; the hot air is heated by an air heater from air separated by an air classifier and an air mill.
(8) Feeding pyrolysis slurry in a pyrolysis tank I into a pyrolysis tank II, wherein the pyrolysis temperature of the pyrolysis tank II is 110 ℃, the pressure is 0.20MPa, and the pyrolysis reaction time is 1.25h; 3000kg/h of raw steam and hot air are sucked into the pyrolysis tank II through a jet stirrer; the hot air is heated by an air heater from air separated by an air classifier and an air mill.
(9) And (3) feeding the pyrolysis slurry in the pyrolysis tank II into a flash tank II, flashing out low-pressure water vapor, wherein the temperature of the flash tank II is 80 ℃, carrying out adiabatic flash evaporation, and enabling the flashed vapor to enter a compressor.
(10) Feeding the pyrolysis slurry subjected to flash evaporation in the flash tank II into a horizontal double-drum centrifuge II for centrifugal separation, feeding separated mother liquor and washing water into a mother liquor and a washing water tank, and cooling CO discharged by a carbonization tank I through a carbonization tank I cooler by the mother liquor and the washing water 2 Then enters a digestion tank I; centrifugally separating out a light magnesium carbonate filter cake by a horizontal double-drum centrifugal machine II; the outer rotary drum of the centrifuge is 2400rpm, the inner rotary drum is 2410rpm, the retention time of the materials in the centrifuge is 5min, and the temperature of the magnesium carbonate filter cake is 70 ℃;
wherein:
(10-1) feeding the filter cake containing the light magnesium carbonate into a hollow blade dryer II through a screw conveyer to dry with 600kg/h of raw steam; the temperature in the hollow blade dryer II is 140 ℃, the pressure is 0.361MPa, and the material residence time is 1.5h; the temperature of the discharged water vapor is 140 ℃, the pressure is 0.361MPa, and the discharged water vapor enters a compressor; the temperature of the steam condensate water discharged by the jacket of the hollow blade dryer II is 140 ℃, and the temperature of the dried magnesium-containing calcium carbonate powder discharged by the hollow blade dryer II is 140 ℃;
(10-2) feeding the dried light magnesium carbonate powder into an air flow mill II for grinding;
and (10-3) feeding the ground light magnesium carbonate powder into an air classifier II for classification, and packaging to leave a factory after classification to obtain the finished light magnesium carbonate powder.
Example 3
The method for producing the light magnesium carbonate based on the recycling utilization based on the device of the embodiment 1 comprises the following steps:
(1) 2189kg/h of raw material low-quality magnesium oxide (mass fraction 60%), mother liquor, washing water and 54045kg/h of heating steam condensate water are fed into a digestion tank I; the digestion temperature of the digestion tank I is 85 ℃, the pressure is 0.35MPa, the digestion reaction time is 0.5h, and the solid-liquid mass ratio is 1:27, secondary steam 221 ℃,0.15MPa,5000kg/h is sucked in by a jet stirrer to directly heat the digestive juice.
(2) Feeding the digestion slurry in the digestion tank I into a digestion tank II, wherein the digestion temperature of the digestion tank II is 90 ℃, the pressure is 0.3MPa, the digestion reaction time is 0.5h, the secondary water vapor is 221 ℃, the pressure is 0.15MPa, and 1700kg/h of the digestion slurry is directly heated by being sucked in by a jet stirrer.
(3) Feeding the digested slurry in the digestion tank II into the carbonization tank I, and sucking CO discharged from the carbonization tank II and the pyrolysis tank I, II 2 A gas; the carbonization temperature of the carbonization tank I is 93 ℃, the pressure is 0.275MPa, the carbonization reaction time is 1.5h, the raw steam is 230 ℃, the pressure is 0.4MPa, the pressure is 760kg/h, and the CO discharged by the carbonization tank II and the pyrolysis tank I, II 2 Sucked into the carbonization tank I through a jet stirrer.
(4) Feeding carbonized slurry in a carbonization tank I into a carbonization tank II, wherein the carbonization temperature of the carbonization tank II is 96 ℃, the pressure is 0.25MPa, the carbonization reaction time is 1h, the raw steam is 1000kg/h, and the fresh CO is fresh 2 270kmol/h (rate of introduction, CO content recovered from light burned magnesia) 2 Gas, CO 2 30% by volume) was sucked into carbonization tank II via a jet stirrer.
(5) And (3) feeding carbonized slurry in the carbonization tank II into a flash tank I, flashing out low-pressure water vapor, wherein the temperature of the flash tank I is 80 ℃, carrying out adiabatic flash evaporation, and feeding the flashed vapor into a compressor.
(6) Feeding carbonized slurry subjected to flash evaporation in a flash evaporation tank I into a horizontal double-drum centrifuge I, and performing centrifugal separation to obtain a magnesium-containing calcium carbonate filter cake and magnesium bicarbonate filtrate; the outer rotary drum of the centrifuge is 2400rpm, the inner rotary drum is 2410rpm, the retention time of the materials in the centrifuge is 5min, and the temperature of the magnesium-containing calcium carbonate filter cake is 70 ℃;
wherein:
(6-1) feeding the magnesium-containing calcium carbonate filter cake into a hollow blade dryer I through a screw conveyor, and drying with 300kg/h of raw steam; the temperature in the hollow blade dryer I is 140 ℃, the pressure is 0.361MPa, and the material residence time is 1.5h; the temperature of the discharged water vapor is 140 ℃, the pressure is 0.361MPa, and the discharged water vapor enters a compressor; the temperature of the steam condensate water discharged by the jacket of the hollow blade dryer I is 140 ℃, and the temperature of the dried magnesium-containing calcium carbonate powder discharged by the hollow blade dryer I is 140 ℃;
(6-2) feeding the dried magnesium-containing calcium carbonate into an air flow mill I for grinding;
and (6-3) feeding the ground magnesium-containing calcium carbonate powder into an air classifier I for classification, and packaging to leave a factory after classification to obtain finished magnesium-containing calcium carbonate powder.
(7) Feeding the magnesium bicarbonate filtrate separated by the horizontal double-drum centrifuge I into a pyrolysis tank I, wherein the pyrolysis temperature of the pyrolysis tank I is 110 ℃, the pressure is 0.25MPa, and the pyrolysis reaction time is 1h; 2400kg/h of raw steam and hot air are sucked into the pyrolysis tank I through the jet stirrer; the hot air is heated by an air heater from air separated by an air classifier and an air mill.
(8) Feeding pyrolysis slurry in a pyrolysis tank I into a pyrolysis tank II, wherein the pyrolysis temperature of the pyrolysis tank II is 115 ℃, the pressure is 0.20MPa, and the pyrolysis reaction time is 1h; 3000kg/h of raw steam and hot air are sucked into the pyrolysis tank II through a jet stirrer; the hot air is heated by an air heater from air separated by an air classifier and an air mill.
(9) And (3) feeding the pyrolysis slurry in the pyrolysis tank II into a flash tank II, flashing out low-pressure water vapor, wherein the temperature of the flash tank II is 80 ℃, carrying out adiabatic flash evaporation, and enabling the flashed vapor to enter a compressor.
(10) Feeding the pyrolysis slurry subjected to flash evaporation in the flash tank II into a horizontal double-drum centrifuge II for centrifugal separation, feeding separated mother liquor and washing water into a mother liquor and a washing water tank, and cooling CO discharged by a carbonization tank I through a carbonization tank I cooler by the mother liquor and the washing water 2 Then enters a digestion tank I; centrifugally separating out a light magnesium carbonate filter cake by a horizontal double-drum centrifugal machine II; the outer rotary drum of the centrifuge is 2400rpm, the inner rotary drum is 2410rpm, the retention time of the materials in the centrifuge is 5min, and the temperature of the magnesium carbonate filter cake is 70 ℃;
wherein:
(10-1) feeding the filter cake containing the light magnesium carbonate into a hollow blade dryer II through a screw conveyer to dry with 600kg/h of raw steam; the temperature in the hollow blade dryer I is 140 ℃, the pressure is 0.361MPa, and the material residence time is 1.5h; the temperature of the discharged water vapor is 140 ℃, the pressure is 0.361MPa, and the discharged water vapor enters a compressor; the temperature of the steam condensate water discharged by the jacket of the hollow blade dryer II is 140 ℃, and the temperature of the dried magnesium-containing calcium carbonate powder discharged by the hollow blade dryer II is 140 ℃;
(10-2) feeding the dried light magnesium carbonate powder into an air flow mill II for grinding;
and (10-3) feeding the ground light magnesium carbonate powder into an air classifier II for classification, and packaging to leave a factory after classification to obtain the finished light magnesium carbonate powder.
According to the light magnesium carbonate production method based on resource utilization, the MVR generates secondary steam as an auxiliary heating source, so that comprehensive energy conservation is realized by 36%; the extraction rate of magnesium oxide is more than 90%, the content of magnesium oxide in 2500kg/h light magnesium carbonate is more than 46.5%, the magnesium oxide is higher than the standard of GB/T27814-2011 superior products, and 1420kg/h byproduct superfine magnesium-containing calcium carbonate is an additive of high polymer materials.
The technical scheme of the invention is explained in the technical scheme, the protection scope of the invention cannot be limited by the technical scheme, and any changes and modifications to the technical scheme according to the technical substance of the invention belong to the protection scope of the technical scheme of the invention.
Claims (9)
1. Light magnesium carbonate apparatus for producing based on resource utilization, its characterized in that: the device comprises a digestion tank I, a digestion tank II, a carbonization tank I, a carbonization tank II and a flash tank which are sequentially connected, wherein the flash tank comprises a flash tank I and a flash tank II, and a pyrolysis tank I and a pyrolysis tank II are arranged between the flash tanks I, II; the flash tanks I, II are respectively connected with centrifuges I, II; the digestion tank I, II is used for performing digestion reaction on materials; the carbonization tank I, II is used for performing carbonization reaction on the digested slurry; the flash tank I is used for flashing carbonized slurry; the centrifugal machine I is used for carrying out solid-liquid separation on the carbonized slurry after flash evaporation; the pyrolysis tank I, II is used for carrying out pyrolysis reaction on the magnesium bicarbonate filtrate separated from the solid and the liquid; the flash tank II is used for flashing pyrolysis slurry; the centrifugal machine II is used for carrying out solid-liquid separation on the pyrolysis slurry subjected to flash evaporation to obtain a light magnesium carbonate filter cake;
wherein the agitators arranged in the digestion tank I, the digestion tank II, the carbonization tank I, the carbonization tank II, the pyrolysis tank I and the pyrolysis tank II are jet agitators; CO of the carbonization tank I 2 The gas inlet is connected with CO of the carbonization tank II and the pyrolysis tank I, II 2 A gas outlet, the carbonization tank I discharges CO in the carbonization tank II and the pyrolysis tank I, II 2 The gas is reaction gas;
the device also comprises a compressor, wherein the input end of the compressor is connected with a flash tank I, II, a dryer I, II, and the output end of the compressor is connected with a digestion tank I, II, so that the steam generated by the flash tank I, II and the steam generated by the dryer I, II for drying the filter cake are collected and then boosted and heated to secondary water vapor, and the secondary water vapor is used as a heat source of the digestion tank I, II;
the device also comprises a dryer I, II, an air flow mill I, II, an air flow classifier I, II, a steam condensate water tank, a mother liquor and a washing water tank; the dryer I, the air flow mill I and the air flow classifier I are used for drying, grinding and classifying the filter cakes separated from the solid and liquid to obtain byproducts; the dryer II, the air flow mill II and the air flow classifier II are used for drying, grinding and classifying the light magnesium carbonate filter cake obtained by solid-liquid separation to obtain a product light magnesium carbonate; the carbonization tank I, II, the pyrolysis tank I, II and the heat source of the dryer I, II are steam;
a cooler is further arranged on the gas discharge pipeline of the carbonization tank I and is used for cooling CO discharged by the carbonization tank I 2 A gas; the pyrolysis tank I, II takes air separated by an air classifier I, II and an air mill I, II as an auxiliary heat source, and an air heater is arranged on an air transmission pipeline;
the input end of the steam condensate water tank is connected with the dryer I, II, the output end of the steam condensate water tank is connected with the centrifuge I, II and the digestion tank I, and the steam condensate water is used for collecting steam condensate water formed in the drying process after raw steam is introduced into the dryer I, II, and the steam condensate water is collected into the steam condensate water tank after being heated by the air heater to serve as washing water of the centrifuge I, II and batching water of the digestion tank I;
the input end of the mother liquor and the washing water tank is connected with the centrifugal machine II, the output end of the mother liquor and the washing water tank is connected with the digestion tank I, the mother liquor and the washing water after being centrifuged by the centrifugal machine II are collected, and the mother liquor and the washing water are cooled by the cooler and are subjected to CO discharged by the carbonization tank I 2 The gas enters a digestion tank I and is used as the ingredient water of the digestion tank I.
2. A method for producing light magnesium carbonate based on resource utilization based on the device of claim 1, which is characterized in that: the method specifically comprises the following steps:
(1) Raw materials of magnesium oxide, mother liquor, washing water and steam condensate water enter a digestion tank I, and secondary steam is directly heated for digestion reaction;
(2) Feeding the digestion slurry in the digestion tank I into the digestion tank II, and directly heating by using secondary water vapor to continue digestion reaction;
(3) Feeding the digestive juice in the digestion tank II into the carbonization tank I, and sucking CO discharged by the carbonization tank II 2 CO discharged by gas, pyrolysis tank I and pyrolysis tank II 2 The gas is directly heated by raw steam to carry out carbonization reaction;
(4) Introducing carbonized slurry in the carbonization tank I into the carbonization tank II, and simultaneously introducing fresh CO 2 Directly heating the gas by using raw steam to continue carbonization reaction;
(5) Feeding carbonized slurry in a carbonization tank II into a flash tank I, and flashing out low-pressure water vapor;
(6) Feeding the carbonized slurry subjected to flash evaporation in the flash evaporation tank I into a centrifugal machine I for centrifugal separation to separate a magnesium-containing calcium carbonate filter cake and magnesium bicarbonate filtrate;
(7) Feeding the magnesium bicarbonate filtrate separated by the centrifugal machine I into a pyrolysis tank I, and simultaneously carrying out pyrolysis reaction on the sucked hot air and raw steam;
(8) Feeding the pyrolysis slurry in the pyrolysis tank I into the pyrolysis tank II, and continuously carrying out pyrolysis reaction by using hot air and raw steam which are sucked in at the same time;
(9) Feeding pyrolysis slurry in a pyrolysis tank II into a flash tank II, and flashing out low-pressure water vapor;
(10) Flash tank IIThe pyrolysis slurry after internal flash evaporation is fed into a centrifugal machine II for centrifugal separation, the separated mother liquor and washing water are fed into a mother liquor and a washing water tank, and the mother liquor and the washing water are cooled by a carbonization tank I cooler to cool CO discharged by a carbonization tank I 2 Then enters a digestion tank I; and (3) centrifugally separating out a light magnesium carbonate filter cake by a centrifugal machine II.
3. The method for producing light magnesium carbonate based on resource utilization according to claim 2, which is characterized in that: the digestion temperature of the digestion tank I in the step (1) is 80-85 ℃, the pressure is 0.35MPa, the digestion reaction time is 0.5-1 h, and the solid-liquid mass ratio is 1: (27-30), sucking secondary water vapor through a jet stirrer to directly heat digestion slurry; the digestion temperature of the digestion tank II in the step (2) is 85-90 ℃, the pressure is 0.3MPa, and the digestion reaction time is 0.5-1 h; the secondary steam is sucked in by a jet stirrer to directly heat the digestive juice.
4. The method for producing light magnesium carbonate based on resource utilization according to claim 2, which is characterized in that: the carbonization temperature of the carbonization tank I in the step (3) is 90-93 ℃, the pressure is 0.275MPa, and the carbonization reaction time is 1-1.5 h; CO discharged from raw steam, carbonization tank II and pyrolysis tank I, II 2 Sucking into a carbonization tank I through a jet stirrer; the carbonization temperature of the carbonization tank II in the step (4) is 93-96 ℃, the pressure is 0.25MPa, the carbonization reaction time is 1-1.5 h, and the raw steam and fresh CO are generated 2 Sucking into carbonization tank II via jet stirrer.
5. The method for producing light magnesium carbonate based on resource utilization according to claim 2, which is characterized in that: in the steps (5) and (9), the flash tank I, II is operated adiabatically at a flash temperature of 80 ℃ and the flash vapor enters the compressor.
6. The method for producing light magnesium carbonate based on resource utilization according to claim 2, which is characterized in that: in the step (7): the pyrolysis temperature of the pyrolysis tank I is 105-110 ℃, the pressure is 0.25MPa, and the pyrolysis reaction time is 1-1.25 h; raw steam and hot air are sucked into the pyrolysis tank I through the jet stirrer; in the step (8): the pyrolysis temperature of the pyrolysis tank II is 110-115 ℃, the pressure is 0.20MPa, and the pyrolysis reaction time is 1-1.25 h; raw steam and hot air are sucked into the pyrolysis tank II through the jet stirrer.
7. The method for producing light magnesium carbonate based on resource utilization according to claim 2, which is characterized in that: in the steps (6) and (10), the centrifugal machine I, II is a horizontal double-drum centrifugal machine, in particular a horizontal double-drum spiral discharge centrifugal machine, the outer drum of the centrifugal machine I, II is 2400rpm, the inner drum is 2410rpm, the retention time of materials in the centrifugal machine is 5min, and the temperature of a magnesium calcium carbonate filter cake and a magnesium carbonate filter cake is 70 ℃; the mother liquor and the washing water separated by the centrifugal machine II are fed into a mother liquor and a washing water tank, and the mother liquor and the washing water cool CO discharged by the carbonization tank I 2 And then enters a digestion tank I.
8. The method for producing light magnesium carbonate based on resource utilization according to claim 2, which is characterized in that: the step (6) further comprises: feeding the magnesium-containing calcium carbonate filter cake into a dryer I through a spiral feeder to be dried by using raw steam; feeding the dried magnesium-containing calcium carbonate into an air flow mill I for grinding; the ground magnesium-containing calcium carbonate powder is fed into an air classifier I for classification, and the classified magnesium-containing calcium carbonate powder is finished and packaged to leave the factory; the step (10) further comprises: feeding the light magnesium carbonate filter cake into a dryer II through a spiral feeder, and drying by using raw steam; feeding the dried light magnesium carbonate powder into an air flow mill II for grinding; and (3) feeding the ground light magnesium carbonate powder into an air classifier II for classification, and packaging to leave a factory after classification to obtain the finished light magnesium carbonate powder.
9. The method for producing light magnesium carbonate based on resource utilization according to claim 8, which is characterized in that: in the steps (6) and (10), the dryer I, II is a hollow blade dryer, a drying heat source is steam, the steam is respectively introduced into a jacket and a hollow blade of the hollow blade dryer I, II, and condensed water of the steam is collected in a steam condensate water tank after being heated by air; the water vapor generated by drying the filter cake is heated and boosted by a compressor to be used as secondary water vapor; the temperature in the dryer I, II is 135-140 ℃, the pressure is 0.313-0.361 MPa, and the material retention time is 0.75-1.5 h; the temperature of the discharged water vapor is 135-140 ℃, and the pressure is 0.313-0.361 MPa; the temperature of the steam condensate discharged by the jacket and the hollow blade of the dryer I, II is 135-140 ℃, and the temperature of the dry material discharged by the hollow blade dryer I, II is 135-140 ℃.
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