CN102515204B - Device for producing salt by brine-mixing and evaporation method with concentrated seawater by-product of seawater desalination as raw material and method thereof - Google Patents
Device for producing salt by brine-mixing and evaporation method with concentrated seawater by-product of seawater desalination as raw material and method thereof Download PDFInfo
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- CN102515204B CN102515204B CN 201110411270 CN201110411270A CN102515204B CN 102515204 B CN102515204 B CN 102515204B CN 201110411270 CN201110411270 CN 201110411270 CN 201110411270 A CN201110411270 A CN 201110411270A CN 102515204 B CN102515204 B CN 102515204B
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Abstract
The invention relates to a device for producing salt by a brine-mixing and evaporation method with a concentrated seawater by-product of seawater desalination as a raw material and a method thereof. The method provided by the invention comprises the following steps of: putting 10 unit volumes of concentrated seawater of 5-12 baume degrees, 2.2-2.5 unit volumes of bitter brine of 28-29 baume degrees and 0.26-0.27 unit volumes of salt slurry into a static mixer H, wherein with the salt slurry as the reference for volume ratio, sodium chloride accounts for 45-50% and bitter brine accounts for 50-55%; mixing brine by the use of the static mixer at room temperature and normal pressure to obtain mixed brine; settling the mixed brine by the use of a settler, forming a solid phase of calcium sulfate, precipitating calcium sulfate from the mixed brine to obtain a calcium sulfate product; allowing the calcium sulfate product to enter into an evaporating pot for evaporation concentration when the concentration of the mixed brine in the settler is baume degrees, continuously precipitating a sodium chloride solid while evaporating water, and carrying out solid-liquid separation on the salt slurry by the use of a centrifuge H to obtain the sodium chloride product. Concentrated seawater discharged from a seawater desalination factory has been completely utilized. Therefore, zero discharge isrealized. Pollution of concentrated seawater to the ocean or occupation of large areas for drying brine is avoided.
Description
Technical field
The present invention relates to the comprehensive utilization of sea water desaltination by-product concentrated seawater, the concentrated seawater that relates in particular to the sea water desaltination by-product is that the device and method of halogen method of evaporation salt manufacturing is converted in the raw material employing.
Background technology
The method that adopts desalination technology to produce fresh water by seawater has been used decades all over the world.In recent years, also obtained fast development in China.
Desalination technology is a large amount of concentrated seawater (the about 5 ° of B é～12 ° B é of concentration) of by-product when producing fresh water, and saltiness is higher 1～3 times than seawater.The concentrated seawater of existing desalinator institute by-product substantially all returns the sea owing to can not solve the calcium sulfate scaling problem when continuing evaporation concentration, and very big pollution is caused in the ocean.
Recent years, domestic newly-built sea water desaltination factory site is all selected to build near the saltern, after concentrated seawater enters the salt pan, (be called for short: Exposure to Sunlight halogen processed) about the concentration enrichment to 25.5 of concentrated seawater ° B é, the calcium sulfate in the concentrated seawater has been separated out more than 85% and is just saturated to sodium-chlor at this moment with the method for Exposure to Sunlight.The saturated bittern of sodium-chlor is introduced in the crystallizing pond method salt manufacturing that with the method salt manufacturing of Exposure to Sunlight, also can introduce factory's usefulness evaporation concentration.
The ocean is polluted or land occupation area Exposure to Sunlight halogen processed for fear of concentrated seawater, Chemicals such as the sodium-chlor that contains in the extraction concentrated seawater, Repone K, magnesium chloride, sal epsom, industrial bromine, calcium sulfate, the various countries expert is studying with the Chemicals in the method extraction concentrated seawater of batch production.But owing to contain a certain amount of calcium sulfate in the concentrated seawater, concentrated seawater can produce calcium sulfate scaling in continuing evaporating concentration process (is called for short: the calcium dirt), cause evaporation unit normally to move.
Summary of the invention
The present invention is according to dissolubility data and the common-ion effcet principle of calcium sulfate in seawater, " converting halogen " method of employing was separated out the calcium sulfate that is dissolved in the concentrated seawater in a large number before advancing evaporating pot, concentrated seawater has successfully been crossed the peak phase that calcium sulfate is separated out, thereby produce the calcium dirt when having avoided concentrated seawater in evaporating pot, to continue evaporation concentration, realized the purpose of concentrated seawater batch production salt manufacturing, concentrated seawater namely need not enter the sea and also not take a large amount of soils.
Technical scheme of the present invention is as follows:
A kind of concentrated seawater with the sea water desaltination by-product is that the device of halogen method of evaporation salt manufacturing is converted in the raw material employing, and static mixer H connects settling vessel C, and settling vessel connects vaporizer Z, and vaporizer connects whizzer L; Static mixer is provided with concentrated seawater entrance H1, bittern entrance H2, salt slurry entrance H4 and mixes halogen outlet H3; Settling vessel is provided with and mixes halogen entrance C1, mixing halogen outlet C2 and calcium sulfate outlet C3; Vaporizer is provided with secondary steam outlet Z1, salt slurry outlet Z2, the outlet of vaporizer bittern Z3, vaporizer mixing halogen entrance Z4, condensation-water drain Z5 and heating steam entrance Z6; Whizzer is provided with whizzer salt slurry entrance L1, salt outlet L2 and whizzer bittern outlet L3; Mixing halogen outlet H3 is connected with mixing halogen entrance C1 through pipeline, mixing halogen outlet C2 is connected with mixing halogen entrance Z4 through pipeline, salt slurry outlet Z2 is connected with the pipeline of salt slurry entrance H4 with whizzer salt slurry entrance L1 through pipeline, mix halogen outlet C2 and be connected with mixing halogen entrance Z4 through pipeline, bittern entrance H2 is connected through the pipeline of pipeline and vaporizer bittern outlet Z3 and whizzer bittern outlet L3.
Concentrated seawater with the sea water desaltination by-product is that raw material adopts the method for halogen method of evaporation salt manufacturing of converting, get 5～12 ° of B é concentrated seawaters of 10 unit volumes and 28～29 ° of B é bitterns of 2.2～2.5 unit volumes and the salt slurry of 0.26～0.27 unit volume and put into static mixer H, the salt slurry is volume ratio; 45～50%, sodium-chlor and 50～55% bitterns; Under normal temperature, normal pressure, convert halogen through static mixer and obtain mixing halogen; Mix halogen through the settling vessel sedimentation, calcium sulfate forms solid phase and separates out from mix halogen, obtains the calcium sulfate product; The mixing halogen concentration of settling vessel is advanced the evaporating pot evaporation concentration when 23～25 ° of B é, solid sodium chloride can constantly be separated out from bittern in transpiring moisture; The salt of getting 0.26～0.27 unit volume of discharging from evaporating pot is starched back the concentrated seawater of converting halogen operation and 10 unit volumes and is converted halogen, and all the other salt slurries obtain the sodium-chlor product after through whizzer H solid-liquid separation; When reaching 28～29 ° of B é, bittern concentration stops evaporation operation, the bittern of getting 2.2～2.5 unit volumes from the bittern that evaporating pot is discharged is got back to the concentrated seawater of converting halogen operation and 10 units and is converted halogen, and all the other bitterns (comprising the bittern that whizzer H discharges) are discharged evaporization process as the raw material of Chemicals such as production Repone K.
So far, the concentrated seawater of discharging from desalinator is all utilized, and accomplishes zero release.
3.3; Advantage of the present invention
Biggest advantage of the present invention is: according to the common-ion effcet principle, getting the bittern (bittern) of high density and salt slurry gets back to and converts the halogen operation and participate in concentrated seawater and convert halogen, separate out with solid phase form being dissolved in the concentrated seawater calcium sulfate dexterously, overwhelming majority calcium sulfate separates with concentrated seawater, reaches concentrated seawater does not generate the calcium dirt when continuing evaporation concentration purpose.Successfully solved concentrated seawater generates the calcium dirt when continuing evaporation concentration a difficult problem, concentrated seawater can realize batch production salt manufacturing, avoided concentrated seawater to the pollution of ocean or taken a large amount of soils shining halogen.
Description of drawings
Fig. 1: apparatus of the present invention figure.
Illustrate:
H: static mixer Z
1: the secondary steam outlet
C: settling vessel Z
2: the outlet of salt slurry
Z: vaporizer Z
3: the outlet of vaporizer bittern
L: whizzer Z
4: vaporizer mixing halogen entrance
H
1: concentrated seawater entrance Z
5: condensation-water drain
H
2: bittern entrance Z
6: the heating steam entrance
H
3: mix halogen outlet L
1: whizzer salt slurry entrance
H
4: salt slurry entrance L
2: the salt outlet
C
1: mix halogen entrance L
3: the outlet of whizzer bittern
C
2: mix the halogen outlet
C
3: the calcium sulfate outlet
Embodiment
Key of the present invention is to adopt the method for converting halogen to solve concentrated seawater to generate the calcium dirt when continuing evaporation concentration, guarantees that evaporation unit moves continuously.
Device of the present invention is as shown in Figure 1: static mixer H connects settling vessel C, and settling vessel connects vaporizer Z, and vaporizer connects whizzer L; Static mixer is provided with concentrated seawater entrance H1, bittern entrance H2, salt slurry entrance H4 and mixes halogen outlet H3; Settling vessel is provided with and mixes halogen entrance C1, mixing halogen outlet C2 and calcium sulfate outlet C3; Vaporizer is provided with secondary steam outlet Z1, salt slurry outlet Z2, the outlet of vaporizer bittern Z3, vaporizer mixing halogen entrance Z4, condensation-water drain Z5 and heating steam entrance Z6; Whizzer is provided with whizzer salt slurry entrance L1, salt outlet L2 and whizzer bittern outlet L3; Mixing halogen outlet H3 is connected with mixing halogen entrance C1 through pipeline, mixing halogen outlet C2 is connected with mixing halogen entrance Z4 through pipeline, salt slurry outlet Z2 is connected with the pipeline of salt slurry entrance H4 with whizzer salt slurry entrance L1 through pipeline, mix halogen outlet C2 and be connected with mixing halogen entrance Z4 through pipeline, bittern entrance H2 is connected through the pipeline of pipeline and vaporizer bittern outlet Z3 and whizzer bittern outlet L3.
Concentrated seawater with the sea water desaltination by-product is that raw material adopts the method for halogen method of evaporation salt manufacturing of converting, get 5～12 ° of B é concentrated seawaters of 10 unit volumes and 28～29 ° of B é bitterns of 2.2～2.5 unit volumes and the salt slurry of 0.26～0.27 unit volume and put into static mixer H, the salt slurry is volume ratio; 45～50%, sodium-chlor and 50～55% bitterns; Under normal temperature, normal pressure, convert halogen through static mixer and obtain mixing halogen; Mix halogen through the settling vessel sedimentation, calcium sulfate forms solid phase and separates out from mix halogen, obtains the calcium sulfate product; The mixing halogen concentration of settling vessel is advanced the evaporating pot evaporation concentration when 23～25 ° of B é, solid sodium chloride can constantly be separated out from bittern in transpiring moisture; The salt of getting 0.26～0.27 unit volume of discharging from evaporating pot is starched back the concentrated seawater of converting halogen operation and 10 unit volumes and is converted halogen, and all the other salt slurries obtain the sodium-chlor product after through whizzer H solid-liquid separation; When reaching 28～29 ° of B é, bittern concentration stops evaporation operation, the bittern of getting 2.2～2.5 unit volumes from the bittern that evaporating pot is discharged is got back to the concentrated seawater of converting halogen operation and 10 units and is converted halogen, and all the other bitterns (comprising the bittern that whizzer H discharges) are discharged evaporization process as the raw material of Chemicals such as production Repone K.
Example 1:
The first step is converted the halogen operation
Get 11～12 ° of B é concentrated seawaters ((salt slurry (volume ratio of sulfur acid calcium 0.30～0.35g/l) and 0.264 liter in this moment bittern of the bittern of sulfur acid calcium 4.03～4.06g/l) and 28～29 ° of B é of 2.4 liters in this moment concentrated seawater of 10 liters; 45～50%, sodium-chlor, 50～55%, bittern) under normal temperature, normal pressure, convert halogen.
Because common-ion effcet, the calcium sulfate in the concentrated seawater forms solid phase and separates out from mix halogen, and through the settling vessel sedimentation, calcium sulfate separates with mixing halogen, isolates 21～23 gram calcium sulfate products.
Through converting mixing halogen concentration after the halogen about 23～25 ° of B é, the calcium sulphate content of this moment has dropped to the 1.40～1.45g/l that mixes halogen (23～25 ° of B é) from 4.03～4.06g/l of concentrated seawater (11～12 ° of B é).
After converting halogen, the halogen operation obtains about 12.4～12.5 liters mixing halogen (concentration is at 23～25 ° of B é) as the raw material of evaporization process through converting.
Second step, evaporization process
The concentration of converting after the halogen enters the evaporization process evaporation concentration at the mixing halogen of 23～25 ° of B é, and bittern concentration stops evaporation when reaching 28～29 ° of B é.
The part (ratio see convert the halogen operation) that evaporization process is discharged bittern is returned and is converted the halogen operation and convert halogen, all the other bitterns (1.5～1.6 liters, sulfur acid calcium 0.30～0.36g/l) are as the raw material of producing product such as Repone K.
A part (ratio see convert the halogen operation) of discharging the salt slurry is returned and is converted that the halogen operation is converted halogen, all the other salt slurries obtain 800～810 gram sodium-chlor products through solid-liquid separation.
Example 2
The first step is converted the halogen operation
Get 9～10B é concentrated seawater ((salt slurry (volume ratio of sulfur acid calcium 0.30～0.35g/l) and 0.264 liter in this moment bittern of the bittern of sulfur acid calcium 3.95～4.02g/l) and 28～29 ° of B é of 2.5 liters in this moment concentrated seawater of 10 liters; 45～50%, sodium-chlor, 50～55%, bittern) under normal temperature, normal pressure, convert halogen.
Because common-ion effcet, the calcium sulfate in the concentrated seawater forms solid phase and separates out from mix halogen, and through the settling vessel sedimentation, calcium sulfate separates with mixing halogen, obtains 20～21 gram calcium sulfate products.
Through converting mixing halogen concentration after the halogen about 23～25 ° of B é, the calcium sulphate content of this moment has dropped to the 1.40～1.45g/l that mixes halogen (23～25 ° of B é) from 3.95～4.03g/l of concentrated seawater (9～10 ° of B é).
After converting halogen, the halogen operation obtains about 12.4～12.5 liters mixing halogen (concentration is at 23～25 ° of B é) as the raw material of evaporization process through converting.
Second step, evaporization process
The mixing halogen of concentration about 23～25 ° of B é of converting after the halogen enters the evaporization process evaporation concentration, and bittern concentration stops evaporation when reaching 28～29 ° of B é.
The part (ratio see convert the halogen operation) that evaporization process is discharged bittern is returned and is converted the halogen operation and convert halogen, all the other bitterns (about 1.45～1.55 liters, sulfur acid calcium 0.30～0.35g/l) are as the raw material of producing product such as Repone K.
A part (ratio see convert the halogen operation) of discharging the salt slurry is returned and is converted that the halogen operation is converted halogen, all the other salt slurries obtain 795～805 gram sodium-chlor products through solid-liquid separation.
The invention solves concentrated seawater and when continuing evaporation concentration, generate the calcium dirt, guarantee that evaporation unit moves continuously.Described in the inventionly can not be interpreted as the restriction that the present invention is done, to belonging to mentality of designing of the present invention on the whole, and the apparent change of having done all should belong within the protection domain of the present invention.
Claims (2)
1. the concentrated seawater with the sea water desaltination by-product is that the device of halogen method of evaporation salt manufacturing is converted in the raw material employing, it is characterized in that static mixer H connects settling vessel C, and settling vessel connects vaporizer Z, and vaporizer connects whizzer L; Static mixer is provided with concentrated seawater entrance H1, bittern entrance H2, salt slurry entrance H4 and mixes halogen outlet H3; Settling vessel is provided with and mixes halogen entrance C1, mixing halogen outlet C2 and calcium sulfate outlet C3; Vaporizer is provided with secondary steam outlet Z1, salt slurry outlet Z2, the outlet of vaporizer bittern Z3, vaporizer mixing halogen entrance Z4, condensation-water drain Z5 and heating steam entrance Z6; Whizzer is provided with whizzer salt slurry entrance L1, salt outlet L2 and whizzer bittern outlet L3; Mixing halogen outlet H3 is connected with mixing halogen entrance C1 through pipeline, mixes halogen outlet C2 and is connected with mixing halogen entrance Z4 through pipeline, and the salt slurry exports Z2 and is connected through the pipeline of pipeline and whizzer salt slurry entrance L1 and salt slurry entrance H4; Bittern entrance H2 is connected with the pipeline of whizzer bittern outlet L3 with vaporizer bittern outlet Z3 through pipeline.
2. the concentrated seawater with the sea water desaltination by-product is that raw material adopts the method for halogen method of evaporation salt manufacturing of converting, it is characterized in that getting 5～12 ° of B é concentrated seawaters of 10 unit volumes and 28～29 ° of B é bitterns of 2.2～2.5 unit volumes and the salt slurry of 0.26～0.27 unit volume and put into static mixer H, the salt slurry is volume ratio; 45～50%, sodium-chlor and 50～55% bitterns; Under normal temperature, normal pressure, convert halogen through static mixer and obtain mixing halogen; Mix halogen through the settling vessel sedimentation, calcium sulfate forms solid phase and separates out from mix halogen, obtains the calcium sulfate product; The mixing halogen concentration of settling vessel is advanced the evaporating pot evaporation concentration when 23～25 ° of B é, solid sodium chloride can constantly be separated out from bittern in transpiring moisture; The salt of getting 0.26～0.27 unit volume of discharging from evaporating pot is starched back the concentrated seawater of converting halogen operation and 10 unit volumes and is converted halogen, and all the other salt slurries obtain the sodium-chlor product after through whizzer H solid-liquid separation; When reaching 28～29 ° of B é, bittern concentration stops evaporation operation, the bittern of getting 2.2～2.5 unit volumes from the bittern that evaporating pot is discharged is got back to the concentrated seawater of converting halogen operation and 10 units and is converted halogen, and all the other bitterns are discharged evaporization process as the raw material of products such as production Repone K.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110411270 CN102515204B (en) | 2011-12-09 | 2011-12-09 | Device for producing salt by brine-mixing and evaporation method with concentrated seawater by-product of seawater desalination as raw material and method thereof |
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| CN 201110411270 CN102515204B (en) | 2011-12-09 | 2011-12-09 | Device for producing salt by brine-mixing and evaporation method with concentrated seawater by-product of seawater desalination as raw material and method thereof |
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| CN102515204A CN102515204A (en) | 2012-06-27 |
| CN102515204B true CN102515204B (en) | 2013-09-25 |
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| CN109534568A (en) * | 2017-09-22 | 2019-03-29 | 金達行有限公司 | Integrated seawater resources utilization system |
| CN111547745A (en) * | 2020-05-18 | 2020-08-18 | 天津君瑞和科技有限公司 | Method for removing sodium chloride from bittern produced by seawater |
| CN111362284A (en) * | 2020-05-18 | 2020-07-03 | 天津君瑞和科技有限公司 | Method for preparing magnesium potassium sulfate from bittern obtained by preparing salt from seawater |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN100410175C (en) * | 2006-08-08 | 2008-08-13 | 杨秀文 | Comprehensive utilization method of sea salt bittern |
| CN101172686A (en) * | 2007-10-18 | 2008-05-07 | 中盐制盐工程技术研究院 | Method for eliminating calcium sulphate with bittern |
| CN101234767A (en) * | 2008-02-29 | 2008-08-06 | 天津长芦海晶集团有限公司 | Thick seawater comprehensive utilization technique after seawater desalination |
| EA201100433A1 (en) * | 2008-09-04 | 2011-10-31 | И.Д.Е. Текнолоджис Лтд. | IMPROVED WATER DECOMPOSITION SYSTEM |
| CN101704560B (en) * | 2009-07-29 | 2011-09-07 | 林晓山 | Technique for desalting sea water, making salt and comprehensively using by-products thereof by utilizing wind energy, solar energy and heat pump technologies |
| CN202390216U (en) * | 2011-12-09 | 2012-08-22 | 吴宗生 | Salt manufacturing device using high concentration seawater of seawater desalination byproduct as raw material by brine mixing evaporating method |
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