CN102311131A - Process for co-producing potassium chloride and sodium chloride by sylvite brine evaporation method - Google Patents
Process for co-producing potassium chloride and sodium chloride by sylvite brine evaporation method Download PDFInfo
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- CN102311131A CN102311131A CN2010102223538A CN201010222353A CN102311131A CN 102311131 A CN102311131 A CN 102311131A CN 2010102223538 A CN2010102223538 A CN 2010102223538A CN 201010222353 A CN201010222353 A CN 201010222353A CN 102311131 A CN102311131 A CN 102311131A
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Abstract
The invention relates to a process for co-producing potassium chloride and sodium chloride by a sylvite brine evaporation method, which comprises the following steps of: (1) salt preparation work procedure through evaporation: the countercurrent multi(4 to 5)-effect evaporation is carried out on underground sylvite brine solution, the evaporation temperature is 40 to 150 DEG C, and then, the solid-liquid separation is carried out to obtain sodium chloride in raw materials and salt preparation mother solution; and (2) potassium chloride preparation work procedure through evaporation: the co-current multi(3 to 4)-effect evaporation is carried out on the salt preparation mother solution, the evaporation temperature is 125 to 40 DEG C, then, the solid-liquid separation is carried out to obtain potassium preparation mother liquid and potassium chloride, and the potassium preparation mother liquid participates in the subsequent circle of the salt preparation work procedure through evaporation. The process has the characteristics that the process flow is refined, the engineering investment is saved, the product quality conforms to national standards, the adaptability of raw materials is high, the cost is low, the energy consumption is low, the three-waste discharge does not exist, and the like.
Description
Technical field
The present invention relates to the technology of a kind of sylvite bittern evaporation method coproduction Repone K and sodium-chlor.
Background technology
Known sylvite is produced the method for Repone K; Mainly contain solid ore deposit thermosol crystallization process; This method existence need be with underground mining sylvite solid ore deposit, the thermosol steam consumption is higher, saliferous mine tailing amount is big and construction investment is big problem; Therefore, Repone K and sodium-chlor economy that aforesaid method separates in the sylvite are relatively poor, have serious environmental protection problem simultaneously.
The present invention is directed to the problems referred to above, the technology of a kind of sylvite bittern evaporation method coproduction Repone K and sodium-chlor is provided.
Goal of the invention
The purpose of this invention is to provide the technology of a kind of sylvite bittern evaporation method coproduction Repone K and sodium-chlor, this technology is easy, reduces investment, energy consumption and cost, solves saliferous mine tailing amount macro-environment protection problem at all.
For reaching the foregoing invention purpose, the present invention adopts following technical scheme:
This sylvite bittern evaporation method coproduction Repone K and sodium-chlor technology, it may further comprise the steps:
(1), evaporation salt manufacturing operation: down-hole sylvite aqueous salt brine is carried out countercurrent multi-effect evaporation, vaporization temperature 40-150 ℃, carry out solid-liquid separation then and obtain sodium-chlor and salt-making mother liquor in the raw material;
(2): above-mentioned salt-making mother liquor is carried out the following current multiple-effect evaporation, vaporization temperature 125-40 ℃, carry out solid-liquid separation then and obtain making potassium mother liquor and Repone K, this system potassium mother liquor is participated in the above-mentioned evaporation salt manufacturing of round-robin operation down.
Contain NaCl 300-1g/l, KCl 10-300g/l in the sylvite bittern of described down-hole
Described salt-making mother liquor contains NaCl 300-250g/l, KCl 160-470g/l.
System potassium mother liquor contains NaCl 250-300g/l, KCl 450-160g/l.
Evaporation salt manufacturing operation can adopt 4-5 to imitate; Evaporation system Repone K operation can adopt 3-4 to imitate.
Described down-hole sylvite bittern system solution can also contain a kind of in calcium sulfate (0.1-5g/l), magnesium chloride (0.1-6g/l), the sal epsom (0.1-1.5g/l) at least.
In the above-mentioned technological process, utilize temperature rising Repone K solubleness to increase, the characteristics that sodium-chlor solubleness reduces; And the employing multiple-effect evaporation, it is little that product per ton consumes steam, and the theoretical recovery of Repone K of the present invention and sodium-chlor is 100%; Product Repone K quality (contains KCl>=93% more than reaching the national GB/T7118-1999 top grade of issuing; NaCl≤1.75%), the product sodium-chlor quality premium grads standard that reaches country promulgation (contains NaCl>=99.1%, SO
4 2-≤0.30%).Technological process does not have waste liquid and discharges, have raw material availability high with the quality product height, energy consumption is low, production cost is low and characteristics such as three-waste free discharge.
Description of drawings
Fig. 1: the process flow sheet of the part evaporation salt manufacturing operation in an embodiment of the present invention and the centrifugal drying operation of product
Fig. 2: evaporate first effect, the 2nd effect evaporation salt producing craft schema that the salt manufacturing operation links to each other with Fig. 1
Fig. 3: the process flow sheet of the evaporation system Repone K operation that links to each other with Fig. 1, Fig. 2
Among Fig. 1, Fig. 2, Fig. 3, EV-201, EV-202, EV-203, EV-204 are the salt manufacturing evaporating pot, their corresponding outfit HE-201, HE-202, HE-203, HE-204 outer heat-exchanger; P-301, P302, P209, P213 are pump, and above-mentioned evaporating pot is serial connection, but the trend of material and steam is for driving in the wrong direction; Sylvite bittern is added to end jar (promptly the 4th jar) earlier, and the steam of boiler is added to first jar earlier, in the mother liquor that first jar is gone out; The content of KCL is the highest, and its discharging is added to first jar that extracts KCL, that is: EV-301 arrives the EV-302 evaporating pot again; In this technology, sylvite bittern is placed among the storage tank T602.The NaCl that above-mentioned EV-201, EV-202, EV-203, EV-204 evaporating pot below emit delivers to devices such as centrifugal separating device TH-401, obtains the NaCl solid at last.Simultaneously, the evaporating pot product in the evaporation system Repone K operation is seen solid K CL to devices such as TH501 spinnings off from rotary conveyor.
Embodiment
Embodiment 1: get 1000m
3NaCl 260g/l, KCl 130g/l down-hole sylvite bittern are raw material, with circulation system potassium mother liquor 859m
3Evaporate, 100 ℃ of vaporization temperatures (first imitates temperature) are carried out solid-liquid separation then and are obtained 260 tons in sodium-chlor and high temperature evaporation salt-making mother liquor 906m in the raw material
3, salt-making mother liquor component (NaCl 274g/l, KCl354g/l), low-temperature evaporation salt-making mother liquor wherein carries out solid-liquid separation and obtains making potassium mother liquor 859m
3With 130 tons in Repone K, 50 ℃ of vaporization temperatures, system potassium mother liquor component (NaCl 289g/l, KCl222g/l), this system potassium mother liquor is participated in the above-mentioned high temperature evaporation salt manufacturing operation of circulation down.
Embodiment 2: get 1000m
3NaCl 300g/l, KCl 160g/l down-hole sylvite bittern are raw material, with circulation system potassium mother liquor 1593m
3Evaporate, 80 ℃ of vaporization temperatures (first imitates temperature) are carried out solid-liquid separation then and are obtained 300 tons in sodium-chlor and high temperature evaporation salt-making mother liquor 1649m in the raw material
3, salt-making mother liquor component (NaCl 282g/l, KCl300g/l), low-temperature evaporation salt-making mother liquor wherein carries out solid-liquid separation and obtains making potassium mother liquor 1593m
3With 160 tons in Repone K, 45 ℃ of vaporization temperatures, system potassium mother liquor component (NaCl 292g/l, KCl210g/l), this system potassium mother liquor is participated in the above-mentioned high temperature evaporation salt manufacturing operation of circulation down.
Embodiment 3: get 1000m
3NaCl 298g/l, KCl 158g/l down-hole sylvite bittern are raw material, with circulation system potassium mother liquor 863m
3Evaporate, 100 ℃ of vaporization temperatures (first imitates temperature) are carried out solid-liquid separation then and are obtained 298 tons in sodium-chlor and high temperature evaporation salt-making mother liquor 929m in the raw material
3, salt-making mother liquor component (NaCl 274g/l, KCl354g/l), low-temperature evaporation salt-making mother liquor wherein carries out solid-liquid separation and obtains making potassium mother liquor 863m
3With 158 tons in Repone K, 40 ℃ of vaporization temperatures, system potassium mother liquor component (NaCl295g/l, KCl198g/l), this system potassium mother liquor is participated in the above-mentioned high temperature evaporation salt manufacturing operation of circulation down.
Claims (6)
1. sylvite bittern evaporation method coproduction Repone K and sodium-chlor technology, it is characterized in that: it may further comprise the steps:
(1), evaporation salt manufacturing operation: down-hole sylvite aqueous salt brine is carried out countercurrent multi-effect evaporation, vaporization temperature 40-150 ℃, carry out solid-liquid separation then and obtain sodium-chlor and salt-making mother liquor in the raw material;
(2) evaporation system Repone K operation: above-mentioned salt-making mother liquor is carried out the following current multiple-effect evaporation, vaporization temperature 125-40 ℃, carry out solid-liquid separation then and obtain making potassium mother liquor and Repone K, this system potassium mother liquor is participated in the above-mentioned evaporation salt manufacturing of round-robin operation down.
2. a kind of sylvite bittern evaporation method coproduction Repone K according to claim 1 and sodium-chlor technology is characterized in that: contain NaCl 300-1g/l, KCl 10-300g/l in the sylvite bittern of described down-hole
3. a kind of sylvite bittern evaporation method coproduction Repone K according to claim 1 and 2 and sodium-chlor technology, it is characterized in that: described salt-making mother liquor contains NaCl 300-250g/l, KCl 160-470g/l.
4. according to claim 1 or 2 or 3 described a kind of sylvite bittern evaporation method coproduction Repone K and sodium-chlor technologies, it is characterized in that: system potassium mother liquor contains NaCl 250-300g/l, KCl 450-160g/l.
5. a kind of sylvite bittern evaporation method coproduction Repone K according to claim 1 and 2 and sodium-chlor technology is characterized in that: described down-hole sylvite bittern system solution also contains a kind of in calcium sulfate, magnesium chloride, the sal epsom at least.
6. a kind of sylvite bittern evaporation method coproduction Repone K according to claim 5 and sodium-chlor technology is characterized in that: described calcium sulfate concentration is that 0.1-5g/l, density of magnesium chloride are that 0.1-6g/l, magnesium sulfate concentration are 0.1-1.5g/l.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2010102223538A CN102311131A (en) | 2010-07-09 | 2010-07-09 | Process for co-producing potassium chloride and sodium chloride by sylvite brine evaporation method |
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| CN2010102223538A CN102311131A (en) | 2010-07-09 | 2010-07-09 | Process for co-producing potassium chloride and sodium chloride by sylvite brine evaporation method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103449478A (en) * | 2013-08-26 | 2013-12-18 | 中盐制盐工程技术研究院 | Comprehensive utilization and production method of underground potassium chloride-rich brine |
| CN105329918A (en) * | 2015-12-02 | 2016-02-17 | 中盐工程技术研究院有限公司 | Eleven-effect combined sodium and potassium preparation device |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4224036A (en) * | 1978-04-03 | 1980-09-23 | Ppg Industries Canada Ltd. | Method of concentrating salt solutions |
| CN1020271C (en) * | 1989-07-13 | 1993-04-14 | 大连皮子窝化工厂 | Technology and apparatus for united production of salt and potassium chloride |
| CN1398784A (en) * | 2002-07-19 | 2003-02-26 | 南风化工集团股份有限公司 | Potassium sulfate producing process |
-
2010
- 2010-07-09 CN CN2010102223538A patent/CN102311131A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4224036A (en) * | 1978-04-03 | 1980-09-23 | Ppg Industries Canada Ltd. | Method of concentrating salt solutions |
| CN1020271C (en) * | 1989-07-13 | 1993-04-14 | 大连皮子窝化工厂 | Technology and apparatus for united production of salt and potassium chloride |
| CN1398784A (en) * | 2002-07-19 | 2003-02-26 | 南风化工集团股份有限公司 | Potassium sulfate producing process |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103449478A (en) * | 2013-08-26 | 2013-12-18 | 中盐制盐工程技术研究院 | Comprehensive utilization and production method of underground potassium chloride-rich brine |
| CN105329918A (en) * | 2015-12-02 | 2016-02-17 | 中盐工程技术研究院有限公司 | Eleven-effect combined sodium and potassium preparation device |
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Application publication date: 20120111 |