CN205709902U - Weight alkali wet decomposition and crystallization tower - Google Patents
Weight alkali wet decomposition and crystallization tower Download PDFInfo
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- CN205709902U CN205709902U CN201620258907.2U CN201620258907U CN205709902U CN 205709902 U CN205709902 U CN 205709902U CN 201620258907 U CN201620258907 U CN 201620258907U CN 205709902 U CN205709902 U CN 205709902U
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Abstract
The utility model discloses a kind of weight alkali wet decomposition and crystallization tower, its tower is made up of up-small and down-big two cylinders, is connected by platform cone transition between two cylinders；Upper cylinder is for decomposing section, and lower cylinder is crystallized region；Decomposing section top and be provided with charging aperture, top is provided with gas outlet, decomposes and is provided with column plate inside section tower body, and bottom is provided with circulation fluid import, and bottom communicates with crystallized region central well down take；Crystallized region top is provided with circulation fluid outlet, and inside is provided with central well down take, and bottom is provided with discharging opening.This utility model is be applicable to the big and heavy alkali of institute's output the production technologies such as union soda, ammonia-soda process, trona carbonization processing method as raw material, through Wet Decomposition, the production of crystallization (or hygroscopic water solution crystallization process) step production high-quality dense soda ash.
Description
Technical field
This utility model relates to the production equipment of a kind of heavy soda ash.The production equipment of heavy soda ash is produced in particular to a kind of sodium bicarbonate.
Background technology
The features such as it is big that heavy soda ash has bulk density, and epigranular is difficult to fly upward, good fluidity, are welcome by soda downstream user deeply.The production method of heavy soda ash, in addition to the U.S. all uses trona monohydrated sodium carbonate (also referred to as monohydrate sodium carbonate) flow process and produces, the light soda ash that other various countries mostly produce with ammonia alkali or connection alkali produces for raw material reprocessing.Processing method has three kinds: solid phase hydration process, liquid phase water be legal and squeezing and pressing method.Wherein in the majority with solid phase hydration process.In three kinds of techniques, production cost is minimum with squeezing and pressing method, and other two kinds of methods are essentially identical；Energy consumption is minimum with squeezing and pressing method, and solid phase hydration process takes second place, and liquid phase water is legal the highest；Product salinity is legal minimum with liquid phase water, and solid phase hydration process, squeezing and pressing method can not reduce the salt content in soda；Squeezing and pressing method product quality is not so good as hydration method.
The process that hydration method produces heavy soda ash is as follows: ammonia alkali or connection alkali carbonating are taken out liquid and obtained wet big and heavy alkali after filtering, and it is with sodium bicarbonate as main component.Weight in wet base alkali is calcined through rotary calcining stove by the steam that pressure is 2.8 ~ 3.2MPa, is decomposed into light sodium carbonate (once calcining)；Light sodium carbonate adds water hydration, generate monohydrated sodium carbonate (being divided into solid phase method and liquid phase method according to the difference of amount of water), monohydrated sodium carbonate calcines (steam pressure is 1.0 ~ 1.3MPa, secondary clacining) through rev again, sloughs and generates heavy soda ash after combining water.Namely hydration method is processed into heavy soda ash by weight in wet base alkali and needs through the monohydrate sodium carbonate stage, be through twice steam calcination.This method long flow path, equipment is many, takes up an area big, and energy consumption is high, simultaneously because rotary calcining stove is poorly sealed, alkali dirt flies upward, severe operational environment.
The process that squeezing and pressing method produces heavy soda ash is as follows: the high temperature light soda ash (calcination product) that ammonia-soda process or union soda produce is passed to cone-type spiral loader via conveying equipment and carries out pre-extrusion, then the light soda ash through pre-extrusion is sent into extruder.Under the effect of extruder pressure roller so that it is density becomes to have the cake block (or stick) of certain mechanical strength, more after crushing and screening, obtains granularity and bulk density satisfactory heavy soda ash product.
Produce soda with trona for Raw material processing and mainly use sodium sesquicarbonate (also referred to as sesquialter alkali) flow process and monohydrate sodium carbonate flow process.Whole world trona is most with the U.S., and integrated distribution, in the Lv He basin of the Wyoming State, belongs to carbonic acid sodium form mineral reserve, and buries shallower, dissolves remove impurity, multiple-effect evaporation, with monohydrate sodium carbonate form crystallization, then obtain heavy soda ash through steam calcination after strip mining transformation.China's trona resource is less, more concentrates with the mineral reserve of Inner Mongol Chagannor and Tongbai Area, henan Province, belongs to bicarbonate sodium form mineral reserve.Hot water is molten adopt after obtain the former halogen that sodium bicarbonate content is higher, after remove impurity through wet decomposition reaction add again Caustic soda neutralize, walk monohydrate sodium carbonate flow process and obtain soda product；Or without hygroscopic water solution, walking sesquialter alkali flow process, the intermediate products obtained are the mixture of sodium sesquicarbonate and monohydrated sodium carbonate, become soda product through steam calcination.The bulk density of sesquialter alkali flow process soda product is relevant to the content of sodium bicarbonate in intermediate products, and through calcining, obtain is light soda ash to sodium bicarbonate, and what monohydrated sodium carbonate calcining obtained is heavy soda ash；In intermediate products, sodium bicarbonate content height then soda product density is little, otherwise the highest.The bulk density of the soda product that employing sodium sesquicarbonate flow process obtains is 0.7～0.8g/cm at present3Between, often do not reach the requirement of heavy soda ash standard.Just can be allowed to be decomposed into sodium carbonate it addition, the sodium bicarbonate in intermediate products has to pass through calcining.Monohydrate sodium carbonate flow process also needs the steam of 1.0 ~ 1.3MPa that monohydrate sodium carbonate carries out calcining to be dried, be allowed to removing and combine water and free water just can obtain heavy soda ash product.
Summary of the invention
The purpose of this utility model: provide a kind of simple in construction, low-pressure steam vapour source can be used, the sodium bicarbonate of continuous operation directly produces the equipment of heavy soda ash, substitutes the complicated and loaded down with trivial details equipment such as calcining furnace, hydration machine (or extruder).
The technical solution of the utility model: a kind of weight alkali wet decomposition and crystallization tower, is made up of up-small and down-big two cylinders, is connected by platform cone transition between two cylinders.Upper cylinder is for decomposing section, and lower cylinder is crystallized region.Decomposing section top and be provided with charging aperture, top is provided with gas outlet, decomposes and is provided with 22 ~ 26 blocks of column plates inside section tower body, and plate spacing 500 ~ 900mm decomposes pars infrasegmentalis and is provided with circulation fluid import, and bottom communicates with crystallized region central well down take.Crystallized region top is provided with circulation fluid outlet, fixed gas air vent and rinse water import, and inside is provided with central well down take, and bottom is provided with discharging opening and drain.
The gas-liquid separation distance of 1.5 ~ 2.5 meters high is had between tower top gas outlet and charging aperture.
The apparent velocity that crystallized region liquid rises is 0.02 ~ 0.08m/s, makes sodium carbonate crystallization be suspended in the bottom of crystallized region.Export the height away from bottom bulkhead under crystallized region central well down take, 1 ~ 4 times of downspout orifice area should be made centered by its annular space area, it is to avoid bottom end socket, solid material is piled up.Crystallized region should have enough solid-liquor separation height, and crystallized region central well down take lower nozzle is edge distance preferably greater than 3 meters under circulation fluid outlet.Acute angle folded by crystallized region magma discharge nozzle and horizontal plane is 45 ~ 60 degree.
The beneficial effects of the utility model: can be to the big and heavy alkali of the production technology institute outputs such as union soda, ammonia-soda process, trona carbonization processing method, the mediation magma formed with heavy soda ash filtrate and a certain amount of supplementary water carries out hygroscopic water solution, make sodium bicarbonate resolution ratio reach 80%～95%, while sodium bicarbonate decomposes, generate sodium carbonate crystallization.It is 130～160 DEG C that crystallized region takes out the temperature of magma, and warm separation obtains the filter cake based on natrium carbonicum calcinatum, it is only necessary to through being dried, and need not calcine and i.e. can get bulk density more than 1.0g/cm3Heavy soda ash.Product quality is equivalent to even above be hydrated method heavy soda ash.
It is lower 10 ~ 30 DEG C than the air outlet temperature of light ash steam roaster that this utility model goes out tower exhaust temperature, and when treating capacity is suitable, compared with light ash calcining furnace, steam used reduces accordingly.Hydration method produces heavy soda ash, adds and combines water and generate monohydrate sodium carbonate, carry out calcining removal the most again and combine water and free water obtains heavy soda ash product after needing thick weight alkali calcining.Crystallization obtained by this utility model is anhydrous alkali, compared with the flow process that hydration method generates heavy soda ash, it is not necessary to providing monohydrate sodium carbonate to decompose heat used, only need to drive away the dry heat of free water, steam consumption reduces.Therefore this utility model energy-saving effect is the most notable, heavy soda ash per ton saves 0.35 ~ 0.5 ton of steam than hydration method heavy soda ash, and have only to≤low pressure (low-grade) steam of 1.0MPa, it is not necessary to the light ash 2.8 ~ 3.2MPa middle pressure steam used by steam roaster.It it is energy-saving and cost-reducing ideal equipment.
This utility model is applicable to the big and heavy alkali of the production technology institute outputs such as union soda, ammonia-soda process, trona carbonization processing method, the mediation magma formed with heavy soda ash filtrate and a certain amount of supplementary water, it is directly produced heavy soda ash, produces intensity and be about 1.4 ~ 1.8 tons of (heavy soda ash)/m3Day.
This utility model instead of light ash calcining furnace, hydration machine or extruder and substantial amounts of solid-handling equipment, and therefore floor space is little, and equipment investment is low, and can reduce the quantity of operator, reduces cost of human resources.Simultaneously because drive apparatus is few, not only decreases power consumption but also decrease leakage, improve labor condition, carry out production strictly in line with rules and regulations for cleaning and lay a good foundation.It it is newly-built, the preferred equipment of reorganization and expansion heavy soda ash device.
Accompanying drawing explanation
Accompanying drawing is attached most importance to the structural representation of alkali wet decomposition and crystallization tower.In figure: 1-crystallized region, 2-central well down take, 3-fixed gas air vent, 4-decomposes section, 5-column plate, and 6-is in harmonious proportion magma charging aperture, 7-offgas outlet, 8-circulation fluid import, 9-rinse water import, and 10-circulation fluid exports, 11-discharging opening, 12-drain.
Detailed description of the invention
This utility model is applicable to produce heavy soda ash flow process for raw material through hygroscopic water solution crystallization process one step with the big and heavy alkali of the production technology outputs such as union soda, ammonia-soda process, trona carbonization processing method, detailed description of the invention is only as a example by the big and heavy alkali of union soda, but the present invention is not limited to example below.
Embodiment one: see accompanying drawing, in figure, weight alkali wet decomposition and crystallization tower is provided with crystallized region 1 and decomposes section 4.The top of crystallized region 1 is provided with circulation fluid outlet 10 and fixed gas air vent 3 and rinse water import 9, and inside is provided with central well down take 2, and bottom is provided with discharging opening 11 and drain 12.The top of central well down take 2 is connected with the bottom decomposing section 4.Decomposing section 4 inside and be provided with column plate 5, top is provided with mediation magma charging aperture 6, and top is provided with offgas outlet 7, and bottom is provided with circulation fluid import 8.
Work process: big and heavy alkali mediation magma is added by the mediation magma charging aperture 6 on the section of decomposition 4 top, from top to bottom through column plate 5, enters into the central well down take 2 of crystallized region 1.In the process, make sodium bicarbonate decompose, and generate sodium carbonate crystallization.Together with the circulating mother liquor come in circulation fluid import 8 by the liquid-solid mixed liquor decomposing section 4, dropping to the bottom of crystallized region 1 through central well down take 2, then the annular space between central well down take 2 and wall rises to the top of crystallized region 1.The apparent velocity that crystallized region liquid rises designs in certain scope, makes sodium carbonate crystallization be suspended in the bottom of crystallized region, and clear liquid is entered into reboiler (being not drawn in figure) by circulation fluid outlet 10.Circulation fluid makes mother solution overheated through reboiler heating, crosses hot mother liquor and is entered into the bottom decomposing section 4 by circulation fluid import 8, and the steam of generation in column plate 5 and liquid-solid material counter current contacting, constantly carries out mass-and heat-transfer from bottom to top.The CO that saturated vapor under certain temperature and pressure produces with weight caustic digestion2And NH3Discharged by tower top offgas outlet 7 together Deng gas.Circulating mother liquor after reboiler heats, makes sodium carbonate liquor produce degree of supersaturation because of vaporizing liquid.During this supersaturated solution flows up between crystallized region wall and central well down take 2 annular space, degree of supersaturation constantly disappears at sodium carbonate crystal surface, makes the crystalline particle suspended in crystallized region grow up.Heavy soda ash magma is taken out by the discharging opening 11 of crystallized region 1 bottom.The fixed gas that crystallized region 1 is assembled is discharged by fixed gas air vent 3.
In the present embodiment: crystallized region 1 diameter 2.6m, high about 7.2m, central well down take diameter 0.7m；Decompose section 4 diameter 1.6m, high about 24.1m, be provided with 25 blocks of column plates 5.Equipment is manufactured by carbon steel, always weighs about 32 tons.Tower top operation pressure ~ 0.025MPa(G), crystallized region temperature 143 ~ 151 DEG C.Used by sizing mixing, big and heavy alkali consists of NH4HCO3
4.40%, Na2CO3
6.00%, NaHCO372.29%, NaCl 0.30%, H2O 17.00%, water the most tolerant 0.01%.The tower magma that enters being in harmonious proportion by big and heavy alkali, heavy soda ash filtrate and supplementary water consists of NH4HCO3
1.21%, Na2CO3
9.84%, NaHCO310.74%, NaCl 2.56%, H2O 53.97%, Na2CO3
(Gu) 10.97%, NaHCO3(Gu) 10.70%, the about 3.2h of the time of staying in tower.Heavy soda ash magma is taken out by the discharging opening 11 of crystallized region 1 bottom, and acute angle folded by discharge nozzle and horizontal plane is 60 degree.The warm filtration of heavy soda ash magma taken out, it is dried and to obtain heavy soda ash product, consisting of Na2CO3
99.07%, NaHCO30.78%, NaCl 0.15%, bulk density 1.04g/cm3, compactness 1.15 g/cm3, mean diameter 0.217mm.
Claims (8)
1. a weight alkali wet decomposition and crystallization tower, it is characterised in that: it is made up of up-small and down-big two cylinders, is connected by platform cone transition between two cylinders；Upper cylinder is for decomposing section, and lower cylinder is crystallized region；Decomposing section top and be provided with charging aperture, top is provided with gas outlet, and inside is provided with column plate, and bottom is provided with circulation fluid import, and bottom communicates with crystallized region central well down take；Crystallized region top is provided with circulation fluid outlet, and inside is provided with central well down take, and bottom is provided with discharging opening.
Heavy alkali the most according to claim 1 wet decomposition and crystallization tower, it is characterised in that counterweight alkali blending liquid carries out hygroscopic water solution, makes sodium bicarbonate resolution ratio reach 80%～95%, generates natrium carbonicum calcinatum crystallization while sodium bicarbonate decomposes.
Heavy alkali the most according to claim 1 wet decomposition and crystallization tower, it is characterised in that the mother solution that the overflow of crystallized region top goes out, mother solution is made to be formed after reboiler heats overheated, produce some vapor, the liquid-solid material counter current contacting got off with upper tray after entering decomposition tower, constantly carry out mass-and heat-transfer.
Heavy alkali the most according to claim 1 wet decomposition and crystallization tower, it is characterised in that the mother solution after reboiler heats, makes sodium carbonate supersaturation because of vaporizing liquid；Crystallized section of central well down take of this supersaturated solution enters into bottom crystallized region, flows up between the annular space of central canal and wall, and degree of supersaturation constantly disappears at sodium carbonate crystal surface, makes the crystalline particle suspended in crystallized region grow up；The apparent velocity that crystallized region liquid rises is 0.02～0.08m/s, makes sodium carbonate crystallization be suspended in the bottom of crystallized region, and crystallized region should have enough solid-liquor separation height, exports under circulation fluid outlet along distance preferably greater than 3 meters under crystallized region central well down take.
Heavy alkali the most according to claim 1 wet decomposition and crystallization tower, it is characterised in that export the height away from crystallized region bottom bulkhead under crystallized region central well down take, should make centered by its annular space area 1～4 times of downspout orifice area.
Heavy alkali the most according to claim 1 wet decomposition and crystallization tower, it is characterised in that acute angle folded by crystallized region magma discharge nozzle and horizontal plane is 45 degree～60 degree；Crystallized region top is provided with fixed gas air vent and rinse water import.
Heavy alkali the most according to claim 1 wet decomposition and crystallization tower, it is characterised in that the temperature of crystallized region discharging magma is 130～160 DEG C, warm separation, obtain the filter cake based on natrium carbonicum calcinatum, it is only necessary to through being dried, need not calcine and i.e. can get bulk density more than 1.0g/cm3Heavy soda ash；It is 1.4～1.8 tons/m that heavy soda ash produces intensity3Day.
Heavy alkali the most according to claim 1 wet decomposition and crystallization tower, it is characterised in that be provided with 22～26 blocks of column plates, plate spacing 500～900mm in decomposing section tower body；The gas-liquid separation distance of 1.5～2.5 meters high is had between tower top gas outlet and charging aperture.
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| CN201620258907.2U CN205709902U (en) | 2016-03-31 | 2016-03-31 | Weight alkali wet decomposition and crystallization tower |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113321259A (en) * | 2021-04-16 | 2021-08-31 | 天华化工机械及自动化研究设计院有限公司 | Energy-saving decarbonization method and system for PTA (pure terephthalic acid) oxidation tail gas washing tower discharge liquid |
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2016
- 2016-03-31 CN CN201620258907.2U patent/CN205709902U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113321259A (en) * | 2021-04-16 | 2021-08-31 | 天华化工机械及自动化研究设计院有限公司 | Energy-saving decarbonization method and system for PTA (pure terephthalic acid) oxidation tail gas washing tower discharge liquid |
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