CN113845131A - Device and method for improving yield of baking soda - Google Patents
Device and method for improving yield of baking soda Download PDFInfo
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- CN113845131A CN113845131A CN202111061725.8A CN202111061725A CN113845131A CN 113845131 A CN113845131 A CN 113845131A CN 202111061725 A CN202111061725 A CN 202111061725A CN 113845131 A CN113845131 A CN 113845131A
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- centrifuge
- sodium bicarbonate
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- crystal slurry
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- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 title claims abstract description 248
- 235000017557 sodium bicarbonate Nutrition 0.000 title claims abstract description 124
- 229910000030 sodium bicarbonate Inorganic materials 0.000 title claims abstract description 124
- 238000000034 method Methods 0.000 title claims abstract description 28
- 239000013078 crystal Substances 0.000 claims abstract description 98
- 238000006243 chemical reaction Methods 0.000 claims abstract description 79
- 239000000706 filtrate Substances 0.000 claims abstract description 78
- 238000003860 storage Methods 0.000 claims abstract description 77
- 239000002245 particle Substances 0.000 claims abstract description 70
- 239000000047 product Substances 0.000 claims abstract description 61
- 239000002002 slurry Substances 0.000 claims abstract description 59
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 52
- 239000012452 mother liquor Substances 0.000 claims abstract description 46
- 238000001816 cooling Methods 0.000 claims abstract description 39
- 238000004519 manufacturing process Methods 0.000 claims abstract description 35
- 239000000463 material Substances 0.000 claims abstract description 33
- 238000001035 drying Methods 0.000 claims abstract description 27
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 26
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 26
- 238000009826 distribution Methods 0.000 claims abstract description 21
- 239000007788 liquid Substances 0.000 claims abstract description 20
- 238000000926 separation method Methods 0.000 claims abstract description 13
- 238000000227 grinding Methods 0.000 claims abstract description 11
- UIIMBOGNXHQVGW-DEQYMQKBSA-M Sodium bicarbonate-14C Chemical compound [Na+].O[14C]([O-])=O UIIMBOGNXHQVGW-DEQYMQKBSA-M 0.000 claims abstract description 7
- 238000003763 carbonization Methods 0.000 claims description 25
- 239000003513 alkali Substances 0.000 claims description 23
- 238000004806 packaging method and process Methods 0.000 claims description 13
- 230000008569 process Effects 0.000 claims description 13
- 238000002425 crystallisation Methods 0.000 claims description 5
- 230000008025 crystallization Effects 0.000 claims description 5
- 238000012216 screening Methods 0.000 claims description 4
- 230000009471 action Effects 0.000 claims description 3
- 230000005484 gravity Effects 0.000 claims description 3
- 239000007791 liquid phase Substances 0.000 claims description 3
- 239000007790 solid phase Substances 0.000 claims description 3
- 238000003756 stirring Methods 0.000 claims description 3
- 230000001376 precipitating effect Effects 0.000 claims 1
- 229940095686 granule product Drugs 0.000 abstract description 16
- 238000010000 carbonizing Methods 0.000 abstract description 4
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 48
- 235000017550 sodium carbonate Nutrition 0.000 description 19
- 229910000029 sodium carbonate Inorganic materials 0.000 description 19
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 11
- 239000011882 ultra-fine particle Substances 0.000 description 6
- 239000002994 raw material Substances 0.000 description 5
- 238000004090 dissolution Methods 0.000 description 4
- 230000009467 reduction Effects 0.000 description 4
- 235000011121 sodium hydroxide Nutrition 0.000 description 4
- 239000008187 granular material Substances 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000005119 centrifugation Methods 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 230000002950 deficient Effects 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 238000001308 synthesis method Methods 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 1
- 238000009621 Solvay process Methods 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- -1 alkali metal bicarbonate Chemical class 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 235000010755 mineral Nutrition 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000010899 nucleation Methods 0.000 description 1
- 230000006911 nucleation Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
- 238000010408 sweeping Methods 0.000 description 1
- 230000008719 thickening Effects 0.000 description 1
- 239000002562 thickening agent Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D7/00—Carbonates of sodium, potassium or alkali metals in general
- C01D7/10—Preparation of bicarbonates from carbonates
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D7/00—Carbonates of sodium, potassium or alkali metals in general
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2004/00—Particle morphology
- C01P2004/51—Particles with a specific particle size distribution
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Abstract
The invention discloses a device and a method for improving the yield of sodium bicarbonate, wherein the device comprises the following steps: comprises a centrifuge filtrate storage tank, a mother liquor pump, a reaction crystallizer, a crystal slurry tank, a crystal slurry pump, a distribution groove, a centrifuge, an air flow dryer, a drying separator, a cooling separator, a rotary screen, a large granule product storage bin, a small granule product storage bin, a grinder and an ultrafine granule product storage bin; injecting filtrate of a centrifuge in the baking soda production device into a filtrate storage tank of the centrifuge, and cooling to obtain mother liquor containing sodium bicarbonate seed crystals; introducing mother liquor and carbon dioxide into the reaction crystallizer, carbonizing and crystallizing, and collecting crystal slurry in a crystal slurry tank; carrying out solid-liquid separation on the crystal mush, wherein wet materials pass through a chute, a spiral conveyor, an airflow dryer, a drying separator and a cooling separator to obtain dry materials; the dried material enters a rotary screen, and the large and small granular sodium bicarbonate which is screened out enters a large and small granular product storage bin respectively; grinding the small-particle sodium bicarbonate to obtain superfine sodium bicarbonate, and putting the superfine sodium bicarbonate into a superfine-particle product storage bin. The sodium bicarbonate has high yield and large product granularity.
Description
Technical Field
The invention belongs to the technical field of baking soda production, and particularly relates to a device and a method for improving baking soda yield.
Background
Baking soda (NaHCO3) is an important inorganic chemical product and has wide application in various industries such as chemical industry, medicine, food, feed, catalyst and the like. The production method of baking soda includes natural soda process, double decomposition process and synthesis process. The synthesis method is a main industrial production method, namely the sodium carbonate is prepared by the carbonation reaction of a sodium carbonate aqueous solution and carbon dioxide gas. At present, the basic process flow of soda production by soda ash carbonation method is that soda ash is used as raw material, and the soda ash is subjected to soda ash dissolution, filtration and impurity removal, carbonization reaction, solid-liquid separation, drying, packaging and the like. The problems that it has are: (1) the baking soda plant built in the soda plant generally adopts sweeping soda, defective soda and the like as raw materials to prepare baking soda. However, with the expansion of the production scale of the baking soda, the raw materials can not meet the requirement, and the baking soda is prepared by carbonizing the raw materials again by using the soda ash finished product with higher cost, so that the waste of energy and resources is caused; (2) the high temperature of the discharge at the bottom of the carbonization tower causes the concentration of sodium bicarbonate in the solution to be high, so the yield is low, and if the alkali is dissolved at the high temperature, the sodium bicarbonate in the solution is decomposed, so the waste of energy is caused; (3) the supersaturation degree of sodium bicarbonate in the carbonization tower is higher, so that the nucleation rate is increased, the crystal growth rate is reduced, and the product has smaller granularity and bad appearance.
With respect to the problem of increasing the yield of baking soda, CN103172090 discloses a process for the production of sodium bicarbonate, which adds sodium sulfate and/or sodium chloride to promote the crystallization of sodium bicarbonate, however, this process introduces impurities. Liu hong Wei (the influence of the operation of a carbonization tower of a baking soda production process on the total alkali amount is firstly detected, Chinese well mineral salt 2015,46,10-12) improves the temperature, the air inflow and the like of the baking soda carbonization tower so as to improve the yield of the baking soda. Great Fengchun and open Shi (a new process for producing baking soda by a synthesis method, modern chemical engineering, 2008,1,69-73.) propose to utilize caustic soda to neutralize sodium bicarbonate in a soda solution, thereby promoting the conversion of sodium carbonate and improving the yield of baking soda. However, the price of caustic soda is high, and the problem of resource waste is also existed when sodium bicarbonate is neutralized by caustic soda.
For the problem of increasing the particle size of baking soda, CN101357770 discloses a method for preparing sodium bicarbonate, which is suitable for an ammonia-soda process device, and uses part of heavy alkali separation mother liquor as a supply liquid of a carbonization tower to perform carbonization reaction by means of two-stage gas inlet, so as to increase the particle size of baking soda from 80-90 μm to 120-150 μm. CN1849263 discloses a process for preparing alkali metal bicarbonate, which utilizes a portion of the magma to be returned to the crystallization device as seed to increase the particle size. CN103303946A discloses a sodium bicarbonate crystal preparation apparatus and a process method for preparing sodium bicarbonate crystals by using the apparatus, wherein the apparatus is a carbonization tower with three reaction zones for preparing large-particle sodium bicarbonate. CN104402023A discloses a production method for increasing the granularity of baking soda products by a carbonization method, which utilizes defective alkali as a raw material, adds baking soda as a seed crystal, thickens the baking soda by a thickener after carbonization reaction, and returns part of the baking soda to a carbonization tower for circulation, thereby producing baking soda products with larger granularity. Machunhua and Lirongjie (introduction of a novel carbonator in the production of baking soda, salt industry and chemical industry, 2015,44(1),5-8.) describe a method for replacing a carbonating tower with a carbonating crystallizer, wherein the carbonating crystallizer is a surface cooling forced circulation crystallizer, and the carbonating reaction is completed in a cooler, so that the baking soda product has larger and uniform granularity.
At present, the conventional synthesis process is adopted by the company, soda coming out of a soda device is added into a soda dissolving tank containing circulating mother liquor for dissolving, the temperature of alkali liquor is kept above 95 ℃, sodium bicarbonate in the circulating mother liquor is decomposed into sodium carbonate, and high-temperature soda dissolving liquor with the concentration of the sodium carbonate reaching 130-150g/L is obtained. Clarifying, filtering, and carbonizing in a carbonizing tower. After carbonization, thickening and centrifugal separation, the filtrate still has certain concentration of sodium carbonate (30-60g/L) and sodium bicarbonate (100-160 g/L). The invention selects the centrifugal filtrate of the alkali liquor discharged from the bottom of the carbonization tower in the production of sodium bicarbonate as the reaction mother liquor. And cooling to separate out sodium bicarbonate fine crystals serving as seed crystals, and then feeding the seed crystals into a reaction crystallizer to react with carbon dioxide. On one hand, sodium carbonate in the mother liquor is further utilized, and the yield is improved on the basis of the original device; on the other hand, the solute is allowed to grow around the seed crystal, resulting in a large particle product.
Disclosure of Invention
The invention aims to overcome the defects in the prior art, provides a device and a method for improving the yield of baking soda, can reduce the concentration of sodium bicarbonate in circulating mother liquor, reduce the temperature of alkali dissolving, save energy, have large product granularity and are suitable for different baking soda production plants.
The purpose of the invention can be realized by the following technical scheme.
The invention relates to a device for improving the yield of baking soda, which comprises a centrifuge filtrate storage tank, a mother liquor pump, a reaction crystallizer, a crystal slurry tank, a crystal slurry pump, a distribution groove, a centrifuge, an air flow dryer, a drying separator, a cooling separator and a rotary screen;
the centrifuge filtrate storage tank is used for storing and cooling the centrifugal filtrate of the alkali liquor discharged from the bottom of the carbonization tower in the baking soda production device, a feed inlet of the centrifuge filtrate storage tank is connected with a centrifugal filtrate pipeline, and a discharge outlet of the centrifuge filtrate storage tank is connected with a feed inlet of a mother liquor pump through a pipeline;
the reaction crystallizer is used for the reaction of mother liquor and carbon dioxide, the reaction crystallizer is of a conical structure with a wide upper part and a narrow lower part, a feed port of the reaction crystallizer is connected with a discharge port of a mother liquor pump through a pipeline, the top of the reaction crystallizer is connected with a vent pipeline, an air inlet at the bottom of the reaction crystallizer is connected with a carbon dioxide pipeline, and the discharge port of the reaction crystallizer is connected with a feed port of a crystal slurry tank through a pipeline; the crystal slurry tank is used for storing crystal slurry, and a discharge port of the crystal slurry tank is connected with a feed port of the crystal slurry pump through a pipeline;
the distribution tank is used for receiving crystal slurry and flowing to the centrifuge under the action of gravity, a feed port of the distribution tank is connected with a discharge port of the crystal slurry pump through a pipeline, and a discharge port of the distribution tank is connected with a feed port of the centrifuge through a pipeline; the centrifuge is used for solid-liquid separation of crystal slurry, a liquid-phase discharge port of the centrifuge is connected to a filtrate storage tank of the centrifuge through a pipeline, and a solid-phase discharge port of the centrifuge is connected with a feed port of the screw conveyor through a chute;
the airflow dryer is used for fully contacting wet materials with hot air to evaporate moisture, the drying separator is used for drying and separating materials, and the cooling separator is used for cooling and separating materials; the feed port of the airflow dryer is connected with the discharge port of the screw conveyor through a pipeline, the discharge port of the airflow dryer is connected with the feed port of the drying separator through a pipeline, and the discharge port of the drying separator is connected with the feed port of the cooling separator through a pipeline;
the rotary screen is used for screening particle materials, the rotary screen feed inlet passes through the discharge gate of pipeline connection cooling separator, the large granule discharge gate and the tiny particle discharge gate of rotary screen pass through the feed inlet of pipeline connection large granule product warehouse and tiny particle product warehouse respectively, large granule product discharge pipeline is connected to the discharge gate in large granule product warehouse and is packed, the discharge gate in tiny particle product warehouse passes through the feed inlet that pipeline connection ground the machine, the discharge gate of grinding the machine passes through the feed inlet of pipeline connection superfine particle product warehouse, superfine product discharge pipeline is connected to the discharge gate in superfine particle product warehouse and is packed.
The centrifuge filtrate storage tank is provided with a cooling device.
The crystal slurry tank is provided with an automatic stirring device.
The purpose of the invention can be realized by the following technical scheme.
The method for improving the yield of the baking soda comprises the following steps:
firstly, centrifuging an alkali liquor discharged from the bottom of a carbonation tower in a sodium bicarbonate production device by using a centrifuge to obtain a filtrate, returning part of the filtrate to the sodium bicarbonate production device for dissolving alkali, injecting part of the filtrate into a filtrate storage tank of the centrifuge, cooling the filtrate in the filtrate storage tank of the centrifuge to 50-65 ℃, and separating out sodium bicarbonate crystals to obtain a mother liquor containing sodium bicarbonate seed crystals;
secondly, introducing mother liquor and carbon dioxide with certain concentration into the reaction crystallizer, carrying out carbonization crystallization, and collecting crystal slurry from the middle lower part of the reaction crystallizer and collecting the crystal slurry by a crystal slurry tank;
thirdly, the crystal slurry in the crystal slurry tank is pumped to a distribution groove by a crystal slurry pump, solid-liquid separation is carried out by a centrifugal machine, the obtained filtrate is returned to a filtrate storage tank of the centrifugal machine, and the obtained wet material sequentially passes through a chute, a screw conveyor, an airflow dryer, a drying separator and a cooling separator to obtain a dried material;
fourthly, the dried material enters a rotary screen, the screened large-particle baking soda enters a large-particle product storage bin for packaging, and meanwhile, the screened small-particle baking soda enters a small-particle product storage bin;
and fifthly, grinding the small-particle sodium bicarbonate by a grinder to obtain superfine sodium bicarbonate, and putting the superfine sodium bicarbonate into a superfine particle product storage bin for packaging.
In the first step, the concentration of sodium carbonate in the filtrate is 30-60g/L, and the concentration of sodium bicarbonate is 100-160g/L
In the second step, the reaction crystallizer is in a tapered structure with a wide upper part and a narrow lower part, and the flow of mother liquor is controlled to be 50-80m by a mother liquor pump3The air input quantity of the/h injected into the reaction crystallizer and the bottom of the reaction crystallizer is 20-40m3The reaction is fully carried out by the carbon dioxide; wherein the concentration of carbon dioxide is 40-65%.
Compared with the prior art, the technical scheme of the invention has the following beneficial effects:
(1) the filtrate of the centrifuge in the baking soda production device is cooled in the filtrate storage tank of the centrifuge, the difference of the solubility of sodium carbonate and sodium bicarbonate in water is utilized, namely, sodium bicarbonate is firstly separated out of crystals in the cooling process, so that the yield is improved, and on the other hand, the mother liquor with sodium bicarbonate crystals is introduced into the reaction crystallizer to react with carbon dioxide, so that the effect of seed crystals is achieved, and the particles of baking soda are enlarged.
(2) In the invention, the cooled mother liquor is injected into a reaction crystallizer from the alkali liquor after carbonization, and is carbonized with carbon dioxide for the second time, and sodium carbonate and sodium bicarbonate in the mother liquor are utilized for the second time. On the basis of the original device, the yield can be improved by 2-4.4 t/h.
(3) The reaction crystallizer is in a conical structure with a wide upper part and a narrow lower part and has a function of grading the granularity, the baking soda crystals with smaller granularity are suspended at the middle upper part of the reaction crystallizer, and the baking soda crystals with larger granularity are settled at the middle lower part of the reaction crystallizer.
(4) According to the invention, the product granularity can be increased without adopting a traditional large-scale carbonization tower for carbonization process flow, the operation is simple, all indexes reach relevant industrial standards, and large-particle sodium bicarbonate products with the particle size of less than 80 meshes can be industrially and continuously produced.
(5) The superfine baking soda is obtained by grinding the small-particle product obtained by rotary screening, so that the product competitiveness is improved, and the product operation range is widened.
Drawings
FIG. 1 is a schematic view showing the structure of the apparatus for increasing the production of sodium bicarbonate according to the present invention.
Figure 2 is a particle size and mass percent distribution plot for the baking soda product produced in example 1.
Figure 3 is a particle size and mass percent distribution plot for the baking soda product produced in example 2.
Figure 4 is a particle size and mass percent distribution plot for the baking soda product produced in example 3.
Reference numerals: 1-centrifuge filtrate storage tank, 2-mother liquor pump, 3-reaction crystallizer, 4-crystal slurry tank, 5-crystal slurry pump, 6-distribution tank, 7-centrifuge, 8-chute, 9-screw conveyor, 10-air flow dryer, 11-drying separator, 12-cooling separator, 13-rotary screen, 14-large granule product storage bin, 15-small granule product storage bin, 16-grinding mill and 17-ultrafine granule product storage bin.
Detailed Description
The invention is further described below with reference to the accompanying drawings.
As shown in figure 1, the device for improving the yield of baking soda mainly comprises a centrifuge filtrate storage tank 1, a mother liquor pump 2, a reaction crystallizer 3, a magma tank 4, a magma pump 5, a distribution tank 6, a centrifuge 7, an air flow dryer 10, a drying separator 11, a cooling separator 12, a rotary screen 13 and the like.
Centrifuge filtrating storage tank 1 is used for storing and cooling the centrifugation filtrating of carbonating tower bottom play alkali lye in the sodium bicarbonate apparatus for producing, centrifuge filtrating storage tank 1's feed inlet is connected with the centrifugation filtrating pipeline, centrifuge filtrating storage tank 1's discharge gate passes through the feed inlet of pipe connection mother liquor pump 2. Wherein, centrifuge filtrate storage tank 1 is provided with a cooling device.
The reaction crystallizer 3 is used for the reaction of mother liquor and carbon dioxide, and the reaction crystallizer 3 is of a conical structure with a wide upper part and a narrow lower part. The feeding port of the reaction crystallizer 3 is connected with the discharging port of the mother liquor pump 2 through a pipeline, the top of the reaction crystallizer 3 is connected with an emptying pipeline, the air inlet at the bottom of the reaction crystallizer 3 is connected with a carbon dioxide pipeline, and the discharging port of the reaction crystallizer 3 is connected with the feeding port of the crystal slurry tank 4 through a pipeline.
Crystal thick liquid jar 4 is used for crystal thick liquid to store, 4 feed inlets of crystal thick liquid jar pass through the pipeline and link to each other with reaction crystallizer 3, the feed inlet of the discharge gate of crystal thick liquid jar 4 through pipe connection crystal thick liquid pump 5. Wherein, the crystal slurry tank 4 is provided with an automatic stirring device.
The distributing groove 6 is used for receiving crystal slurry and flows to the centrifuge 7 through the action of gravity, the feed inlet of the distributing groove 6 passes through the discharge hole of the pipeline connection crystal slurry pump 5, and the discharge hole of the distributing groove 6 passes through the feed inlet of the pipeline connection centrifuge 7.
The centrifuge 7 is used for solid-liquid separation of crystal slurry, the feed inlet of the centrifuge 7 is connected with the distribution groove 6 through a pipeline, the liquid phase discharge outlet of the centrifuge 7 is connected to the centrifuge filtrate storage tank 1 through a pipeline, and the solid phase discharge outlet of the centrifuge 7 is connected with the feed inlet of the screw conveyer 9 through the chute 8.
The pneumatic dryer 10 is used for wet material and hot air to fully contact and evaporate moisture, the feed inlet of the pneumatic dryer 10 is connected with the discharge hole of the screw conveyor 9 through a pipeline, and the discharge hole of the pneumatic dryer 10 is connected with the feed inlet of the drying separator 11 through a pipeline.
The drying separator 11 is used for drying and separating materials, a feed inlet of the drying separator 11 is connected with the airflow dryer 10 through a pipeline, and a discharge outlet of the drying separator 11 is connected with a feed inlet of the cooling separator 12 through a pipeline.
The cooling separator 12 is used for cooling and separating materials, a feed inlet of the cooling separator 12 is connected with the drying separator 11 through a pipeline, and a discharge outlet of the cooling separator 12 is connected with the rotary screen 13 through a pipeline.
The rotary screen 13 is used for screening particle materials, a feed inlet of the rotary screen 13 is connected with a discharge outlet of the cooling separator 12 through a pipeline, and a large particle discharge outlet and a small particle discharge outlet of the rotary screen 13 are respectively connected with feed inlets of a large particle product storage bin 14 and a small particle product storage bin 15 through pipelines.
The large granule product storage bin 14 is used for storing large granule products, the feed inlet of the large granule product storage bin 14 is connected with the rotary screen 13 through a pipeline, and the discharge outlet of the large granule product storage bin 14 is connected with a large granule product discharge pipeline for packaging.
The small granule product storage bin 15 is used for storing small granule products, the feed inlet of the small granule product storage bin 15 is connected with the rotary screen 13 through a pipeline, and the discharge outlet of the small granule product storage bin 15 is connected with the feed inlet of the grinding machine 16 through a pipeline.
The grinder 16 is used for grinding the small-particle products into ultrafine-particle products, a feed inlet of the grinder 16 is connected with the small-particle product storage bin 15 through a pipeline, and a discharge outlet of the grinder 16 is connected with a feed inlet of the ultrafine-particle product storage bin 17 through a pipeline.
The superfine particle product storage bin 17 is used for storing superfine particle products, a feed inlet of the superfine particle product storage bin 17 passes through a pipeline and the grinding machine 16, and a discharge outlet of the superfine particle product storage bin 17 is connected with a superfine product discharge pipeline for packaging.
The method for improving the yield of the baking soda comprises the following steps:
firstly, centrifuging an alkali liquor discharged from the bottom of a carbonization tower in a baking soda production device by a centrifuge to obtain a filtrate, returning part of the filtrate of the centrifuge to the baking soda production device for dissolving alkali, injecting part of the filtrate into a filtrate storage tank 1 of the centrifuge, cooling the filtrate in the filtrate storage tank 1 of the centrifuge to 50-65 ℃, and separating out sodium bicarbonate crystals by utilizing the change of the solubility of sodium bicarbonate along with the change of temperature to obtain a mother liquor containing sodium bicarbonate seed crystals. Wherein, the concentration of sodium carbonate in the filtrate of the centrifuge in the baking soda production device is 30-60g/L, and the concentration of sodium bicarbonate is 100-160 g/L.
And secondly, introducing mother liquor and carbon dioxide with a certain concentration into the reaction crystallizer 3, carrying out carbonization crystallization, and collecting crystal slurry from the middle lower part of the reaction crystallizer 3 by a crystal slurry tank 4.
Specifically, the flow of the mother liquor after temperature reduction is controlled to be 50-80m by a mother liquor pump 23The air input of the reaction crystallizer 3 with the conical structure with the wide upper part and the narrow lower part injected into the reaction crystallizer 3 and the bottom of the reaction crystallizer 3 is 20-40m3The reaction of the carbon dioxide is fully carried out, and crystal mush is extracted from the middle lower part of the reaction crystallizer 3 and collected by the crystal mush tank 4. Wherein the carbon dioxide content is 40-65%.
And thirdly, conveying the crystal slurry in the crystal slurry tank 4 to a distribution tank 6 by a crystal slurry pump 5, performing solid-liquid separation by a centrifuge 7, returning the obtained filtrate to a centrifuge filtrate storage tank 1, and sequentially passing the obtained wet material through a chute 8, a screw conveyor 9, an airflow dryer 10, a drying separator 11 and a cooling separator 12 to obtain the dried material.
In the fourth step, the dried material enters the rotary screen 13, the screened large-particle (180-.
In a fifth step, the small particle baking soda is ground by grinder 16 to obtain ultra-fine (<28 μm) baking soda, which is then fed to an ultra-fine particle product storage bin 17 for packaging.
Example 1
(1) The alkali liquor discharged from the bottom of a carbonization tower in the conventional baking soda production device of the company is treated by a centrifuge to obtain filtrate (30 g/L of sodium carbonate and 100g/L of sodium bicarbonate), one part of the filtrate is returned to the baking soda production device for alkali dissolution, the other part of the filtrate is injected into a centrifuge filtrate storage tank 1, the filtrate is cooled to 50 ℃ in the centrifuge filtrate storage tank 1, and sodium bicarbonate crystals are separated out to obtain mother liquor containing sodium bicarbonate crystal seeds.
(2) The mother liquor after temperature reduction is pumped by a mother liquor pump 2 for 50m3The flow of the reaction crystallizer 3 is sent to the reaction crystallizer 3, and the air input quantity of the reaction crystallizer 3 and the bottom is 20m3The reaction of the carbon dioxide is fully carried out, the crystal mush after the reaction is extracted from the middle lower part of the reaction crystallizer 3, and the extracted liquid is collected by the crystal mush tank 4. Wherein the concentration of carbon dioxide is 40%.
(3) The crystal slurry in the crystal slurry tank 4 is sent to a distribution groove 6 by a crystal slurry pump 5, solid-liquid separation is carried out by a centrifugal machine 7, the obtained filtrate is returned to a filtrate storage tank 1 of the centrifugal machine, and the obtained wet material passes through a chute 8, a spiral conveyor 9, an air flow dryer 10, a drying separator 11 and a cooling separator 12 in sequence to obtain the dried material.
(4) The dried material enters a rotary screen 13, and the screened-out large-particle (180-.
(5) The small particle baking soda is ground by grinder 16 to obtain ultra-fine (<28 μm) baking soda, which is then sent to ultra-fine particle product storage 17 and packaged in a packaging shop.
Detected, with reference to fig. 2: the obtained product has a mass content of <80 meshes (particle size >180 μm) > 75%, a mass content of 40-80 meshes (180 μm < particle size <425 μm) > 20%, and a mass content of <40 meshes (particle size >425 μm) > 50%. The embodiment can obtain the yield of 2t/h, and the product index reaches the industrial standard.
Example 2
(1) The alkali liquor discharged from the bottom of a carbonization tower in the conventional baking soda production device of the company is treated by a centrifuge to obtain filtrate (sodium carbonate: 60g/L and sodium bicarbonate: 160g/L), one part of the filtrate is returned to the baking soda production device for alkali dissolution, the other part of the filtrate is injected into a centrifuge filtrate storage tank 1, the filtrate is cooled to 65 ℃ in the centrifuge filtrate storage tank 1, and sodium bicarbonate crystals are separated out to obtain mother liquor containing sodium bicarbonate crystal seeds.
(2) The mother liquor after temperature reduction is pumped by a mother liquor pump 280m3The flow of the reaction crystallizer 3 is sent to the reaction crystallizer 3, and the air input quantity of the reaction crystallizer 3 and the bottom is 40m3The reaction of the carbon dioxide is fully carried out, the crystal mush after the reaction is extracted from the middle lower part of the reaction crystallizer 3, and the extracted liquid is collected by the crystal mush tank 4. Wherein the concentration of carbon dioxide is 65%.
(3) The crystal slurry in the crystal slurry tank 4 is sent to a distribution groove 6 by a crystal slurry pump 5, solid-liquid separation is carried out by a centrifugal machine 7, the obtained filtrate is returned to a filtrate storage tank 1 of the centrifugal machine, and the obtained wet material passes through a chute 8, a spiral conveyor 9, an air flow dryer 10, a drying separator 11 and a cooling separator 12 in sequence to obtain the dried material.
(4) The dried material enters a rotary screen 13, and the screened-out large-particle (180-.
(5) The small particle baking soda is ground by grinder 16 to obtain ultra-fine (<28 μm) baking soda, which is then sent to ultra-fine particle product storage 17 and packaged in a packaging shop.
Detected, with reference to fig. 3: the obtained product has a mass content of <80 meshes (particle size >180 μm) > 75%, a mass content of 40-80 meshes (180 μm < particle size <425 μm) > 15%, and a mass content of <40 meshes (particle size >425 μm) > 60%. The embodiment can obtain the yield of 4.4t/h, and the product index reaches the industrial standard.
Example 3
(1) The alkali liquor discharged from the bottom of a carbonization tower in the conventional baking soda production device of the company is treated by a centrifuge to obtain filtrate (sodium carbonate: 45g/L and sodium bicarbonate: 130g/L), one part of the filtrate is returned to the baking soda production device for alkali dissolution, the other part of the filtrate is injected into a centrifuge filtrate storage tank 1, the filtrate is cooled to 60 ℃ in the centrifuge filtrate storage tank 1, and sodium bicarbonate crystals are separated out to obtain mother liquor containing sodium bicarbonate crystal seeds.
(2) The mother liquor after temperature reduction is pumped by a mother liquor pump 2 at a speed of 65m3The flow of the reaction crystallizer 3 is sent to the reaction crystallizer 3, and the air input quantity of the reaction crystallizer 3 and the bottom is 30m3The reaction of the carbon dioxide is fully carried out, the crystal mush after the reaction is extracted from the middle lower part of the reaction crystallizer 3, and the extracted liquid is collected by the crystal mush tank 4. Wherein the carbon dioxide concentration is55％。
(3) The crystal slurry in the crystal slurry tank 4 is sent to a distribution groove 6 by a crystal slurry pump 5, solid-liquid separation is carried out by a centrifugal machine 7, the obtained filtrate is returned to a filtrate storage tank 1 of the centrifugal machine, and the obtained wet material passes through a chute 8, a spiral conveyor 9, an air flow dryer 10, a drying separator 11 and a cooling separator 12 in sequence to obtain the dried material.
(4) The dried material enters a rotary screen 13, and the screened-out large-particle (180-.
(5) The small particle baking soda is ground by grinder 16 to obtain ultra-fine (<28 μm) baking soda, which is then sent to ultra-fine particle product storage 17 and packaged in a packaging shop.
Detected, with reference to fig. 4: the obtained product has a mass content of <80 meshes (particle size >180 μm) > 70%, a mass content of 40-80 meshes (180 μm < particle size <425 μm) > 15%, and a mass content of <40 meshes (particle size >425 μm) > 55%. The embodiment can obtain the yield of 3.2t/h, and the product index reaches the industrial standard.
While the present invention has been described in terms of its functions and operations with reference to the accompanying drawings, it is to be understood that the invention is not limited to the precise functions and operations described above, and that the above-described embodiments are illustrative rather than restrictive, and that various changes and modifications may be effected therein by one skilled in the art without departing from the scope or spirit of the invention as defined by the appended claims.
Claims (6)
1. The device for improving the yield of baking soda is characterized by comprising a centrifuge filtrate storage tank (1), a mother liquor pump (2), a reaction crystallizer (3), a crystal slurry tank (4), a crystal slurry pump (5), a distribution tank (6), a centrifuge (7), an air flow dryer (10), a drying separator (11), a cooling separator (12) and a rotary screen (13);
the centrifuge filtrate storage tank (1) is used for storing and cooling the centrifugal filtrate of the alkali liquor discharged from the bottom of the carbonization tower in the baking soda production device, a feed inlet of the centrifuge filtrate storage tank (1) is connected with a centrifugal filtrate pipeline, and a discharge outlet of the centrifuge filtrate storage tank (1) is connected with a feed inlet of the mother liquor pump (2) through a pipeline;
the reaction crystallizer (3) is used for the reaction of mother liquor and carbon dioxide, the reaction crystallizer (3) is of a conical structure with a wide upper part and a narrow lower part, a feed inlet of the reaction crystallizer (3) is connected with a discharge outlet of a mother liquor pump (2) through a pipeline, the top of the reaction crystallizer (3) is connected with a vent pipeline, an air inlet at the bottom of the reaction crystallizer (3) is connected with a carbon dioxide pipeline, and a discharge outlet of the reaction crystallizer (3) is connected with a feed inlet of a crystal slurry tank (4) through a pipeline; the crystal slurry tank (4) is used for storing crystal slurry, and a discharge hole of the crystal slurry tank (4) is connected with a feed hole of the crystal slurry pump (5) through a pipeline;
the distribution groove (6) is used for receiving crystal slurry and flowing to the centrifuge (7) through the action of gravity, a feed inlet of the distribution groove (6) is connected with a discharge outlet of the crystal slurry pump (5) through a pipeline, and a discharge outlet of the distribution groove (6) is connected with a feed inlet of the centrifuge (7) through a pipeline; the centrifuge (7) is used for solid-liquid separation of crystal slurry, a liquid phase discharge port of the centrifuge (7) is connected to a centrifuge filtrate storage tank (1) through a pipeline, and a solid phase discharge port of the centrifuge (7) is connected with a feed port of a screw conveyor (9) through a chute (8);
the airflow dryer (10) is used for fully contacting wet materials with hot air to evaporate moisture, the drying separator (11) is used for drying and separating materials, and the cooling separator (12) is used for cooling and separating materials; the feed inlet of the airflow dryer (10) is connected with the discharge outlet of the screw conveyor (9) through a pipeline, the discharge outlet of the airflow dryer (10) is connected with the feed inlet of the drying separator (11) through a pipeline, and the discharge outlet of the drying separator (11) is connected with the feed inlet of the cooling separator (12) through a pipeline;
the rotary screen (13) is used for screening particle materials, the discharge hole of the feed inlet of the rotary screen (13) passes through a pipeline connecting cooling separator (12), the large particle discharge hole and the small particle discharge hole of the rotary screen (13) respectively pass through the feed inlets of a pipeline connecting large particle product storage bin (14) and a small particle product storage bin (15), the discharge hole of the large particle product storage bin (14) is connected with a large particle product discharge pipeline for packaging, the discharge hole of the small particle product storage bin (15) passes through the feed inlet of a pipeline connecting grinding machine (16), the discharge hole of the grinding machine (16) passes through the feed inlet of a pipeline connecting superfine particle product storage bin (17), and the discharge hole of the superfine particle product storage bin (17) is connected with a superfine product discharge pipeline for packaging.
2. The apparatus for increasing baking soda production according to claim 1, characterized in that the centrifuge filtrate storage tank (1) is provided with cooling means.
3. The apparatus for increasing the production of baking soda according to claim 1, characterized in that the slurry tank (4) is provided with an automatic stirring device.
4. A method for increasing baking soda production based on the baking soda production increasing device of any one of the preceding claims 1 to 3, characterized by comprising the following processes:
firstly, centrifuging an alkali liquor discharged from the bottom of a carbonation tower in a sodium bicarbonate production device by using a centrifuge to obtain a filtrate, returning part of the filtrate to the sodium bicarbonate production device for dissolving alkali, injecting part of the filtrate into a filtrate storage tank (1) of the centrifuge, cooling the filtrate in the filtrate storage tank (1) of the centrifuge to 50-65 ℃, and precipitating sodium bicarbonate crystals to obtain a mother liquor containing sodium bicarbonate seed crystals;
secondly, introducing mother liquor and carbon dioxide with certain concentration into the reaction crystallizer (3) for carbonization and crystallization, and collecting crystal slurry from the middle lower part of the reaction crystallizer (3) and collecting the crystal slurry by a crystal slurry tank (4);
thirdly, conveying the crystal slurry in the crystal slurry tank (4) to a distribution tank (6) by a crystal slurry pump (5), performing solid-liquid separation by a centrifuge (7), returning the obtained filtrate to a centrifuge filtrate storage tank (1), and sequentially passing the obtained wet material through a chute (8), a screw conveyor (9), an airflow dryer (10), a drying separator (11) and a cooling separator (12) to obtain a dried material;
fourthly, the dried material enters a rotary screen (13), the screened large-particle sodium bicarbonate enters a large-particle product storage bin (14) for packaging, and meanwhile, the screened small-particle sodium bicarbonate enters a small-particle product storage bin (15);
and fifthly, grinding the small-particle sodium bicarbonate by a grinder (16) to obtain superfine sodium bicarbonate, and putting the superfine sodium bicarbonate into a superfine particle product storage bin (17) for packaging.
5. The method for increasing the production of sodium bicarbonate according to claim 4, wherein the concentration of sodium bicarbonate in the filtrate in the first step is 30-60g/L, and the concentration of sodium bicarbonate is 100-160 g/L.
6. The process for the production of baking soda according to claim 4, characterized in that in the second step the reaction crystallizer (3) is of a tapered structure with a wide top and a narrow bottom, and the flow rate of mother liquor is controlled by a mother liquor pump (2) to be 50-80m3The air input quantity of the gas injected into the reaction crystallizer (3) and the bottom of the reaction crystallizer (3) is 20-40m3The reaction is fully carried out by the carbon dioxide; wherein the concentration of carbon dioxide is 40-65%.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105819471A (en) * | 2016-05-25 | 2016-08-03 | 天津渤化永利化工股份有限公司 | Method for producing baking soda large in particle size |
| CN111634928A (en) * | 2020-05-14 | 2020-09-08 | 山东海天生物化工有限公司 | Method for preparing large-particle baking soda by secondary carbonization method and baking soda obtained by method |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105819471A (en) * | 2016-05-25 | 2016-08-03 | 天津渤化永利化工股份有限公司 | Method for producing baking soda large in particle size |
| CN111634928A (en) * | 2020-05-14 | 2020-09-08 | 山东海天生物化工有限公司 | Method for preparing large-particle baking soda by secondary carbonization method and baking soda obtained by method |
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