CN103028343B - A kind of production method of pelletoidal calcium chloride dihydrate - Google Patents
A kind of production method of pelletoidal calcium chloride dihydrate Download PDFInfo
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- CN103028343B CN103028343B CN201210549392.8A CN201210549392A CN103028343B CN 103028343 B CN103028343 B CN 103028343B CN 201210549392 A CN201210549392 A CN 201210549392A CN 103028343 B CN103028343 B CN 103028343B
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Abstract
The invention discloses a kind of production method of pelletoidal calcium chloride dihydrate, step: enter in many pelletizing unit bed granulator by the calcium chloride water of 65% ~ 72% through atomizer; Seed particles enters in bed granulator; To enter in bed granulator through atomizer after atomization gas heating and calcium chloride water atomization is coated to seed particles surface; Fluidized gas heating passes in bed granulator, makes calcium chloride water dry, the crystallization being rapidly coated in seed particles surface after atomization; Particle is constantly grown up by granularity during multiple pelletizing unit successively, discharges continuously from discharging port of fluidized bed; The present invention uses high calcium chloride concentration solution, and in bed granulator, dehydrating amount is few, uses the temperature of fluidized gas lower, makes fluid bed unit are production intensity large.Lower atomization gas gas speed, mist torch penetration power is low, can use lower fluid bed bed, reduce fluidized gas bed resistance, and energy consumption, power consumption, plant investment are all significantly reduced.
Description
Technical field
The present invention relates to the production method of inorganic salts calcium chloride, particularly a kind of production method utilizing the pelletoidal calcium chloride dihydrate of fluidized bed granulation process.
Background technology
Calcium chloride product specification has calcium chloride dihydrate and anhydrous calcium chloride two kinds, and product appearance has sheet, pelletiod, bulk and powdery four kinds.Wherein, pelletiod calcium chloride product has that product design is attractive in appearance, good fluidity, do not play dirt, do not lump, the not easily advantage such as moisture absorption, be expected to the main flow kind becoming calcium chloride product.Because existing pelletiod Calcium Chloride Production technology production cost is higher, comparatively sheet calcium chloride dihydrate product price is high by 50% ~ 120% to make pelletoidal calcium chloride dihydrate product price, and calcium chloride dihydrate product more than 90% is in the market still sheet.
Summary of the invention
The object of the invention is the deficiency overcoming the production pelletiod calcium chloride high cost existed in prior art, a kind of production method of pelletoidal calcium chloride dihydrate is provided.
Technical scheme of the present invention is summarized as follows:
A production method for pelletoidal calcium chloride dihydrate, comprises the steps:
Through evaporating the calcium chloride water transport pump that the mass concentration obtained is 65% ~ 72%, enter in many pelletizing unit bed granulator through atomizer;
Seed particles enters in described many pelletizing unit bed granulator by crystal seed feed bin continuously; The atomization gas supplied by Roots blower to enter in described many pelletizing unit bed granulator through atomizer and described calcium chloride water atomization is coated to seed particles surface after First Heat Exchanger is heated to 170 ~ 210 DEG C;
The fluidized gas supplied by air blast passes in described many pelletizing unit bed granulator through inlet for fluidization air after the second heat exchanger is heated to 110 DEG C ~ 150 DEG C, makes calcium chloride water dry, the crystallization being rapidly coated in seed particles surface after atomization; Particle is constantly grown up by granularity during multiple pelletizing unit successively, discharges continuously from discharging port of fluidized bed; Control the discharge rate of discharging port of fluidized bed particle to ensure that described many pelletizing unit bed granulator endoparticle bed height is for 300 ~ 700mm; The particle of being discharged by discharging port of fluidized bed is delivered in screening machine through the first bucket elevator, through secondary screening, the particle being greater than qualified particle diameter is delivered to crystal seed feed bin through the second bucket elevator and is made crystal seed after crusher in crushing together with the particle of the particle and a part of qualified particle diameter that are less than qualified particle diameter; The pelletoidal calcium chloride dihydrate particle of the qualified particle diameter of another part delivers to product feed bin after the cooling of rotating cylinder cooler, and fluid bed tail gas is emptying after leading to scrubbing tower water washing dedust.
Many pelletizing unit bed granulator comprises housing, gas distribution grid and atomizer; Housing is divided into the bed body on top and the air chamber of bottom by the gas distribution grid being arranged on described housing middle and lower part, and the sidewall of air chamber is provided with inlet for fluidization air; The top of bed body is provided with air outlet, and the bottom of bed body sidewall is provided with crystal seed import, and the bottom of the bed body sidewall relative with crystal seed import is provided with discharging port of fluidized bed; Rectangular gas distribution grid is provided with some row's atomizers, often arrange the atomizer Heterogeneous Permutation between atomizer, be spouted district in each atomizer peripheral circular region, the surrounding in spouted district is the outside fluidization regions for rectangle, each atomizer, spouted district and fluidization regions form a pelletizing unit, and each pelletizing unit area is 0.07 ~ 0.15m
2, wherein, region area shared by spouted district is 1/6 ~ 1/2 of fluidization regions; Gas distribution grid adopts porous plate, and wherein, spouted district is different with fluidization regions distribution of gas packing free ratio, makes spouted district gas superficial flow velocity be 2 ~ 4 times of fluidization regions; In spouted district, aperture is vertical with gas distribution grid is arranged; In fluidization regions, aperture and gas distribution grid are that 60 ~ 80 ° of angles are arranged and discharging port of fluidized bed direction is pointed in direction; Described atomizer comprises the gas nozzle with tubular ring, is provided with the fluid injector with helical duct in the inside of described gas nozzle.
The mass concentration entering calcium chloride water in many pelletizing unit bed granulator is 65% ~ 72%, and temperature is 166 DEG C ~ 172 DEG C.
Entering atomization gas pressure in many pelletizing unit bed granulator is 20 ~ 60kPa, and temperature is 170 ~ 210 DEG C.
Advantage of the present invention:
The mass concentration of liquid charging calcium chloride water of the present invention is 65% ~ 72%, and in many pelletizing unit bed granulator, dehydrating amount is few, uses the temperature of fluidized gas lower, makes fluid bed unit are production intensity large.The present invention adopts lower atomization gas gas speed, and mist torch penetration power is low, can use lower fluidized bed layer height, reduce fluidized gas bed resistance.Lower fluidized gas, atomization gas pressure, significantly reduce fluidized gas, atomization gas power of fan.Method of the present invention is compared with existing production technology, and energy consumption, power consumption, plant investment all significantly reduce, and production cost is suitable with existing sheet calcium chloride dihydrate.
The fluid bed of many pelletizing unit bed granulator of the present invention is made up of multiple pelletizing unit, can implement device production capacity expand by increasing pelletizing unit number.Therefore, method amplification risk of the present invention is little, is applicable to large-scale industrial production.
Accompanying drawing explanation
Fig. 1 is FB(flow block);
Fig. 2 is many pelletizing unit bed granulator schematic diagram;
Fig. 3 is the distribution grid schematic diagram of the fluid bed of 15 pelletizing unit, illustrates region shared by each pelletizing unit in figure with dotted line.
Detailed description of the invention
Below by specific embodiments and the drawings, the present invention is further illustrated.
Embodiment 1
A production method for pelletoidal calcium chloride dihydrate, comprises the steps:
Be 70 ~ 71% through evaporating the mass concentration that obtains, temperature is the calcium chloride water transport pump of 169 DEG C ~ 172 DEG C, enters in many pelletizing unit bed granulator through atomizer, and control pressure after calcium chloride water charge pump pump is 0.26MPa simultaneously; Seed particles enters in described many pelletizing unit bed granulator by crystal seed feed bin continuously, and controlling crystal seed returning charge amount is 1.5:1 with the ratio of product yield; The atomization gas supplied by Roots blower to enter in many pelletizing unit bed granulator through atomizer and described calcium chloride water atomization is coated to seed particles surface after First Heat Exchanger is heated to 190 DEG C-210 DEG C, controls atomization gas pressure 55 ~ 60kPa; The fluidized gas supplied by air blast passes in described many pelletizing unit bed granulator through inlet for fluidization air after the second heat exchanger is heated to 110 ~ 120 DEG C, controlling fluidized gas speed in fluid bed is 1.7 ~ 1.9m/s, is coated in calcium chloride water dry, the crystallization rapidly on seed particles surface after atomization; Particle is constantly grown up by granularity during multiple pelletizing unit successively, discharges continuously from discharging port of fluidized bed; Control the discharge rate of discharging port of fluidized bed particle to ensure that described many pelletizing unit bed granulator endoparticle bed height is for 450mm, now bed pressure drop is 3.5kPa; The particle of being discharged by discharging port of fluidized bed is delivered in screening machine through the first bucket elevator, through secondary screening, the particle being greater than qualified particle diameter is delivered to crystal seed feed bin through the second bucket elevator and is made crystal seed after crusher in crushing together with the particle of the particle and a part of qualified particle diameter that are less than qualified particle diameter; The pelletoidal calcium chloride dihydrate particle of the qualified particle diameter of another part delivers to product feed bin after the cooling of rotating cylinder cooler, and fluid bed tail gas is emptying after leading to scrubbing tower water washing dedust.After stable, fluid bed bed temperature is about 90 ~ 100 DEG C, and product calcium chloride content is 74% ~ 75%; , the output of each nozzle is about 300 ~ 330kg/h.(see figure 1)
Described many pelletizing unit bed granulator comprises housing, gas distribution grid 1 and atomizer 10; Housing is divided into the bed body 2 on top and the air chamber 3 of bottom by the gas distribution grid 1 being arranged on described housing middle and lower part, the sidewall of air chamber is provided with inlet for fluidization air 6; The top of bed body is provided with air outlet 9, and the bottom of bed body sidewall is provided with crystal seed import 4, and the bottom of the bed body sidewall relative with crystal seed import is provided with discharging port of fluidized bed 5; Rectangular gas distribution grid is provided with some row's atomizers 10, often arrange the atomizer Heterogeneous Permutation between atomizer, be spouted district 11 in each atomizer peripheral circular region, the surrounding in spouted district is the outside fluidization regions 12 for rectangle, each atomizer, spouted district and fluidization regions form a pelletizing unit, and each pelletizing unit area is 0.07m
2-0.10m
2, wherein, region area shared by spouted district is the 1/3-1/2 of fluidization regions; Spouted district is different with fluidization regions distribution of gas packing free ratio, makes spouted district gas superficial flow velocity be 3 times of fluidization regions; In spouted district, aperture is vertical with gas distribution grid is arranged; In fluidization regions, aperture and gas distribution grid are that 70 ° of angles are arranged and discharging port of fluidized bed direction is pointed in direction; Described atomizer comprises the gas nozzle 13 with tubular ring, is provided with the fluid injector 14 with helical duct in the inside of described gas nozzle.(see Fig. 2 and Fig. 3)
Embodiment 2
A production method for pelletoidal calcium chloride dihydrate, comprises the steps:
Through evaporate the mass concentration that obtains be 65 ~ 67% temperature be the calcium chloride water transport pump of 166 DEG C ~ 168 DEG C, enter in many pelletizing unit bed granulator through atomizer, after control calcium chloride water charge pump pump, pressure is 0.27MPa simultaneously, seed particles enters in described many pelletizing unit bed granulator by crystal seed feed bin continuously, and controlling crystal seed returning charge amount is 0.5:1 with the ratio of product yield; The atomization gas supplied by Roots blower to enter in many pelletizing unit bed granulator through atomizer and described calcium chloride water atomization is coated to seed particles surface after First Heat Exchanger is heated to 170 ~ 180 DEG C, controls atomization gas pressure 20 ~ 30kPa; The fluidized gas supplied by air blast passes in described many pelletizing unit bed granulator through inlet for fluidization air after the second heat exchanger is heated to 145 DEG C ~ 150 DEG C, and the fluidized gas speed in fluid bed that controls is 2.7 ~ 3m/s; Calcium chloride water dry, the crystallization rapidly on seed particles surface is coated in after atomization; Particle is constantly grown up by granularity during multiple pelletizing unit successively, discharges continuously from discharging port of fluidized bed; Control the discharge rate of discharging port of fluidized bed particle to ensure that described many pelletizing unit bed granulator endoparticle bed height is, 300mm, now bed pressure drop is 3kPa; The particle of being discharged by discharging port of fluidized bed is delivered in screening machine through the first bucket elevator, through secondary screening, the particle being greater than qualified particle diameter is delivered to crystal seed feed bin through the second bucket elevator and is made crystal seed after crusher in crushing together with the particle of the particle and a part of qualified particle diameter that are less than qualified particle diameter; The pelletoidal calcium chloride dihydrate particle of the qualified particle diameter of another part delivers to product feed bin after the cooling of rotating cylinder cooler, and fluid bed tail gas is emptying after leading to scrubbing tower water washing dedust.After stable, fluid bed bed temperature is about 120 ~ 130 DEG C, and product calcium chloride content is 82% ~ 84%, and the output of each nozzle is about 350 ~ 380kg/h.
Described many pelletizing unit bed granulator comprises housing, gas distribution grid 1 and atomizer 10; Housing is divided into the bed body 2 on top and the air chamber 3 of bottom by the gas distribution grid 1 being arranged on described housing middle and lower part, the sidewall of air chamber is provided with inlet for fluidization air 6; The top of bed body is provided with air outlet 9, and the bottom of bed body sidewall is provided with crystal seed import 4, and the bottom of the bed body sidewall relative with crystal seed import is provided with discharging port of fluidized bed 5; Rectangular gas distribution grid is provided with some row's atomizers 10, often arrange the atomizer Heterogeneous Permutation between atomizer, be spouted district 11 in each atomizer peripheral circular region, the surrounding in spouted district is the outside fluidization regions 12 for rectangle, each atomizer, spouted district and fluidization regions form a pelletizing unit, and each pelletizing unit area is 0.10m
2-0.13m
2, wherein, region area shared by spouted district is the 1/4-1/6 of fluidization regions; Spouted district is different with fluidization regions distribution of gas packing free ratio, makes spouted district gas superficial flow velocity be 4 times of fluidization regions; In spouted district, aperture is vertical with gas distribution grid is arranged; In fluidization regions, aperture and gas distribution grid are that 60 ° of angles are arranged and discharging port of fluidized bed direction is pointed in direction; Described atomizer comprises the gas nozzle 13 with tubular ring, is provided with the fluid injector 14 with helical duct in the inside of described gas nozzle.
Embodiment 3
A production method for pelletoidal calcium chloride dihydrate, comprises the steps:
Through evaporate the mass concentration that obtains be 72% temperature be 169 DEG C ~ 172 DEG C calcium chloride water transport pump, enter in many pelletizing unit bed granulator through atomizer, after control calcium chloride water charge pump pump, pressure is 0.4MPa simultaneously, seed particles enters in described many pelletizing unit bed granulator by crystal seed feed bin continuously, and controlling crystal seed returning charge amount is 1:1 with the ratio of product yield; The atomization gas supplied by Roots blower to enter in many pelletizing unit bed granulator through atomizer and described calcium chloride water atomization is coated to seed particles surface after First Heat Exchanger is heated to 190 ~ 200 DEG C, controls atomization gas pressure 40 ~ 50kPa; The fluidized gas supplied by air blast passes in described many pelletizing unit bed granulator through inlet for fluidization air after the second heat exchanger is heated to 120 DEG C ~ 130 DEG C, and the fluidized gas speed in fluid bed that controls is 2.3 ~ 2.5m/s.Calcium chloride water dry, the crystallization rapidly on seed particles surface is coated in after atomization; Particle is constantly grown up by granularity during multiple pelletizing unit successively, discharges continuously from discharging port of fluidized bed; Control the discharge rate of discharging port of fluidized bed particle to ensure that described many pelletizing unit bed granulator endoparticle bed height is for 700mm, now bed pressure drop is 6kPa; The particle of being discharged by discharging port of fluidized bed is delivered in screening machine through the first bucket elevator, through secondary screening, the particle being greater than qualified particle diameter is delivered to crystal seed feed bin through the second bucket elevator and is made crystal seed after crusher in crushing together with the particle of the particle and a part of qualified particle diameter that are less than qualified particle diameter; The pelletoidal calcium chloride dihydrate particle of the qualified particle diameter of another part delivers to product feed bin after the cooling of rotating cylinder cooler, and fluid bed tail gas is emptying after leading to scrubbing tower water washing dedust.After stable, fluid bed bed temperature is about 110 ~ 120 DEG C, and product calcium chloride content is 78% ~ 80%.The output of each nozzle is about 570 ~ 600kg/h.
Described many pelletizing unit bed granulator comprises housing, gas distribution grid 1 and atomizer 10; Housing is divided into the bed body 2 on top and the air chamber 3 of bottom by the gas distribution grid 1 being arranged on described housing middle and lower part, the sidewall of air chamber is provided with inlet for fluidization air 6; The top of bed body is provided with air outlet 9, and the bottom of bed body sidewall is provided with crystal seed import 4, and the bottom of the bed body sidewall relative with crystal seed import is provided with discharging port of fluidized bed 5; Rectangular gas distribution grid is provided with some row's atomizers 10, often arrange the atomizer Heterogeneous Permutation between atomizer, be spouted district 11 in each atomizer peripheral circular region, the surrounding in spouted district is the outside fluidization regions 12 for rectangle, each atomizer, spouted district and fluidization regions form a pelletizing unit, and each pelletizing unit area is 0.11m
2-0.15m
2, wherein, region area shared by spouted district is the 1/4-1/6 of fluidization regions; Spouted district is different with fluidization regions distribution of gas packing free ratio, makes spouted district gas superficial flow velocity be 2 times of fluidization regions; In spouted district, aperture is vertical with gas distribution grid is arranged; In fluidization regions, aperture and gas distribution grid are that 80 ° of angles are arranged and discharging port of fluidized bed direction is pointed in direction; Described atomizer comprises the gas nozzle 13 with tubular ring, is provided with the fluid injector 14 with helical duct in the inside of described gas nozzle.
Claims (1)
1. a production method for pelletoidal calcium chloride dihydrate, is characterized in that comprising the steps:
Through evaporating the calcium chloride water transport pump that the mass concentration obtained is 65% ~ 72%, enter in many pelletizing unit bed granulator through atomizer;
Seed particles enters in described many pelletizing unit bed granulator by crystal seed feed bin continuously; The atomization gas supplied by Roots blower to enter in described many pelletizing unit bed granulator through atomizer and described calcium chloride water atomization is coated to seed particles surface after First Heat Exchanger is heated to 170 ~ 210 DEG C;
The fluidized gas supplied by air blast passes in described many pelletizing unit bed granulator through inlet for fluidization air after the second heat exchanger is heated to 110 DEG C ~ 150 DEG C, makes calcium chloride water dry, the crystallization being rapidly coated in seed particles surface after atomization; Particle is constantly grown up by granularity during multiple pelletizing unit successively, discharges continuously from discharging port of fluidized bed; Control the discharge rate of discharging port of fluidized bed particle to ensure that described many pelletizing unit bed granulator endoparticle bed height is for 300 ~ 700mm; The particle of being discharged by discharging port of fluidized bed is delivered in screening machine through the first bucket elevator, through secondary screening, the particle being greater than qualified particle diameter is delivered to crystal seed feed bin through the second bucket elevator and is made crystal seed after crusher in crushing together with the particle of the particle and a part of qualified particle diameter that are less than qualified particle diameter; The pelletoidal calcium chloride dihydrate particle of the qualified particle diameter of another part delivers to product feed bin after the cooling of rotating cylinder cooler, and fluid bed tail gas is emptying after leading to scrubbing tower water washing dedust;
Described many pelletizing unit bed granulator comprises housing, gas distribution grid and atomizer; Housing is divided into the bed body on top and the air chamber of bottom by the gas distribution grid being arranged on described housing middle and lower part, and the sidewall of air chamber is provided with inlet for fluidization air; The top of bed body is provided with air outlet, and the bottom of bed body sidewall is provided with crystal seed import, and the bottom of the bed body sidewall relative with crystal seed import is provided with discharging port of fluidized bed; Rectangular gas distribution grid is provided with some row's atomizers, often arrange the atomizer Heterogeneous Permutation between atomizer, be spouted district in each atomizer peripheral circular region, the surrounding in spouted district is the outside fluidization regions for rectangle, each atomizer, spouted district and fluidization regions form a pelletizing unit, and each pelletizing unit area is 0.07 ~ 0.15m
2, wherein, region area shared by spouted district is 1/6 ~ 1/2 of fluidization regions; Gas distribution grid adopts porous plate, and wherein, spouted district is different with fluidization regions distribution of gas packing free ratio, makes spouted district gas superficial flow velocity be 2 ~ 4 times of fluidization regions; In spouted district, aperture is vertical with gas distribution grid is arranged; In fluidization regions, aperture and gas distribution grid are that 60 ~ 80 ° of angles are arranged and discharging port of fluidized bed direction is pointed in direction; Described atomizer comprises the gas nozzle with tubular ring, is provided with the fluid injector with helical duct in the inside of described gas nozzle;
Entering calcium chloride water mass concentration in many pelletizing unit bed granulator is 65% ~ 72%, and temperature is 166 DEG C ~ 172 DEG C;
Entering atomization gas pressure in many pelletizing unit bed granulator is 20 ~ 60kPa, and temperature is 170 ~ 210 DEG C.
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| CN103922370B (en) * | 2014-04-30 | 2016-03-16 | 刘清山 | Graininess magnesium chloride manufacture method and device |
| CN110116996A (en) * | 2019-06-24 | 2019-08-13 | 乐山师范学院 | A kind of device and method for being granulated crystallization and preparing solid phosphoric acid |
| CN111908495B (en) * | 2020-08-11 | 2022-10-11 | 山东天力能源股份有限公司 | Production process of spherical calcium chloride dihydrate |
| CN114345233B (en) * | 2021-12-20 | 2023-08-22 | 山东天力能源股份有限公司 | Spray granulation device and atomization method suitable for high-concentration calcium chloride solution |
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| JP4162837B2 (en) * | 2000-07-03 | 2008-10-08 | アイテック有限会社 | Calcium chloride hydrate granulator and granulation method |
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| JP4298032B2 (en) * | 1999-01-13 | 2009-07-15 | アイテック有限会社 | Method and apparatus for granulating calcium chloride hydrate |
| CN1377877A (en) * | 2001-04-05 | 2002-11-06 | 中国石油化工股份有限公司巴陵分公司 | Process for producing large particle urea using finished ureea of prilling tower as seed crystal |
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| JP4162837B2 (en) * | 2000-07-03 | 2008-10-08 | アイテック有限会社 | Calcium chloride hydrate granulator and granulation method |
| CN1408469A (en) * | 2002-09-24 | 2003-04-09 | 天津大学 | Jet drive fluidized bed pelletizing device with multiple jet drive units |
| CN101698145A (en) * | 2009-11-11 | 2010-04-28 | 王新月 | Fluidized bed guniting granulation continuous production method |
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