CN109626688A - It is a kind of do not purify under the conditions of middle less salt nitre compare brine concentration method - Google Patents
It is a kind of do not purify under the conditions of middle less salt nitre compare brine concentration method Download PDFInfo
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- CN109626688A CN109626688A CN201811504278.7A CN201811504278A CN109626688A CN 109626688 A CN109626688 A CN 109626688A CN 201811504278 A CN201811504278 A CN 201811504278A CN 109626688 A CN109626688 A CN 109626688A
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- brine
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/68—Treatment of water, waste water, or sewage by addition of specified substances, e.g. trace elements, for ameliorating potable water
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- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
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Abstract
Middle less salt nitre under the conditions of not purifying the invention discloses one kind compares brine concentration method, specifically includes the following steps: S1, less salt nitre compares brine in acquirement, centering less salt nitre is screened than brine, it is repeatedly screened using screening machine, less salt nitre is screened out than the impurity in brine, it obtains the middle less salt nitre without sundries and compares brine, S2, middle less salt nitre after screening is obtained to the component of 75KG -100KG than brine, and it is poured into high-temperature evaporator, brine is stirred, high-temperature evaporator is powered, brine in high-temperature evaporator is heated, S3, in limewash of the middle less salt nitre than 5KG -15KG is added in brine, and the brine after addition limewash is stirred, the present invention relates to brine concentration technique fields.The process that the middle less salt nitre under the conditions of not purifying needs to operate than brine concentration method, by simplifying brine concentration, reduces the loss of energy in brine operating process, purifies when concentration.
Description
Technical field
The present invention relates to brine concentration technique field, the middle less salt nitre under the conditions of specially one kind does not purify is concentrated than brine
Method.
Background technique
The very strong water of mineralising, common to extract certain industrial chemicals, such as salt, iodine, boron, bromine, the scientific name of brine is salt
Halogen, is the mixture of magnesium chloride, magnesium sulfate and sodium chloride, brine order bean curd be colloidal coagulation process, do not occurred chemical anti-
It answers, it is the process of solute and solvent portion separation, concentration process that concentration, which is that the unit operation of partial solvent is removed from solution,
In, moisture removes after borrowing Convention diffusion effect to reach liquid phase surface inside liquid phase inside material, final moisture mass fraction
About 30%, generally stable state evaporate solvent and improve the concentration of solution, refer to unwanted part and reduce and need portion
The relative amount divided increases, and is mainly used for chemical industry term.
Existing brine often requires to be concentrated again after first being purified brine when being concentrated,
The degree of purity of brine is improved, but such mode process is relatively complicated, wastes energy more in brine, increases more
Operating time, reduce operating efficiency.
Summary of the invention
(1) the technical issues of solving
In view of the deficiencies of the prior art, the middle less salt nitre under the conditions of not purifying the present invention provides one kind is than brine concentration side
Method, it is relatively complicated to solve operational sequence, wastes more energy, operating time longer problem.
(2) technical solution
In order to achieve the above object, the present invention is achieved by the following technical programs: one kind do not purify under the conditions of in it is low
Sal prunella than brine concentration method, specifically includes the following steps:
Less salt nitre is screened than brine, centering less salt nitre than brine in S1, acquirement, is repeatedly sieved using screening machine
Choosing, screens out middle less salt nitre than the impurity in brine, obtains the middle less salt nitre without sundries and compares brine；
S2, the component that the middle less salt nitre after screening is obtained to 75KG -100KG than brine, and it is poured into high-temperature evaporator
In, brine is stirred, high-temperature evaporator is powered, the brine in high-temperature evaporator is heated；
S3, it is carried out in limewash of the middle less salt nitre than 5KG -15KG is added in brine, and to the brine after addition limewash
Stirring, mixing time are 15-30 minutes, and the temperature heated at this time is 10 °-20 °, makes the calcium hydroxide and brine in limewash
In magnesium ion (Mg2) reaction, generate magnesium hydrate precipitate, at this time remove brine in magnesium ion (Mg2), excessive hydroxide
Calcium (Ca (0H) 2) is by sodium sulphate (Na2S04) causticization in brine at sodium hydroxide (NaOH)；
S4, in removing the brine after magnesium ion (Mg), be passed through flue gas, and be stirred, mixing time be 15-30
Minute, it reacts carbon dioxide (CO2) and the sodium hydroxide after causticization in brine in flue gas and generates sodium carbonate, sodium carbonate is again
It is reacted with the calcium ion (Ca) in brine and generates calcium carbonate (CaCO3) precipitating, remove the calcium ion (Ca2) contained in brine；
S5,20-35KG of sodium hydroxide solution is added, the temperature of high-temperature evaporator is adjusted to 80 DEG C, is added at the same time
10-15KG of flocculant, it is lasting to stir, it is stood using 25-35 DEG C of temperature, obtains that upper layer is clear halogen, bottom is calcium and magnesium
The suspension of deposit；
S6, clear halogen is extracted, calcium-magnesium-containing sediment turbid liquid is taken out there are mud discharge port is taken out in high-temperature evaporator bottom
Enter slurry tank, sediment squeezing is regarded into fertilizer application at cake；
S7, clear halogen is slowly evaporated using high-temperature evaporator, evaporation time is 1-2 hours, and evaporating temperature is 35-55
DEG C, the brine after being concentrated.
Preferably, limewash is added in the brine is emulsified lime slurry, active calcium oxide in the lime slurry
(Ca0) content is 140-220t, and relative density is 1.2 to 1.4g/cm, and the additional amount of lime slurry controls the hydrogen in brine
The concentration of sodium oxide molybdena (Na0H) is 0.05 to 0.3g/L.
Preferably, the lime slurry is in lime plus water forms, in lime slurry preparation the water that is added be fresh water or
Person's brine.
Preferably, the flocculant added in the step S3 is cationic-type polyacrylamide, and additive amount is 1 to 5ppm.
Preferably, the flue gas being passed through in the brine is generated in boiler using fuel such as heavy oil, natural gas, coals
Flue gas is slowly introducing in brine at normal temperatures and pressures, and the carbon dioxide in flue gas is made to react generation with the brine in S4
The reaction of excessive sodium hydroxide generate sodium carbonate, the intake of flue gas controls between the PH=9 to 12.5 of brine, and raw
At excess of sodium carbonate concentration be 0.1 to 0.8g/L.
Preferably, the flue gas is the clean flue gas by purified treatment, and purification process includes: washing, cooling
And compression.
(3) beneficial effect
Middle less salt nitre under the conditions of not purifying the present invention provides one kind compares brine concentration method.Have compared with prior art
It is standby following the utility model has the advantages that specifically includes the following steps: less salt nitre is sieved than brine, centering less salt nitre than brine in S1, acquirement
Choosing, is repeatedly screened using screening machine, screens out middle less salt nitre than the impurity in brine, and the middle less salt nitre ratio without sundries is obtained
Brine, S2, the component that the middle less salt nitre after screening is obtained to 75KG -100KG than brine, and be poured into high-temperature evaporator,
Brine is stirred, high-temperature evaporator is powered, the brine in high-temperature evaporator is heated, S3, in middle less salt
Limewash of the nitre than 5KG -15KG is added in brine, keeps the magnesium ion (Mg2) in the calcium hydroxide and brine in limewash anti-
It answers, generates magnesium hydrate precipitate, remove the magnesium ion (Mg2) in brine at this time, excessive calcium hydroxide (Ca (0H) 2) is by brine
In sodium sulphate (Na2S04) causticization at sodium hydroxide (NaOH), S4, in removing the brine after magnesium ion (Mg) is passed through flue
Gas, and be stirred, it reacts carbon dioxide (CO2) and the sodium hydroxide after causticization in brine in flue gas and generates carbonic acid
Sodium, sodium carbonate is reacted with the calcium ion (Ca) in brine again generates calcium carbonate (CaCO3) precipitating, remove in brine the calcium that contains from
Sub (Ca2) S5, is added 20-35KG of sodium hydroxide solution, S6, extracts clear halogen, and there are take out mud for high-temperature evaporator bottom
S7, discharge port is slowly evaporated clear halogen using high-temperature evaporator, evaporation time is 1-2 hours, and evaporating temperature is 35-55 DEG C,
Brine after being concentrated, the process for needing to operate by simplifying brine concentration, reduces energy in brine operating process
Loss purifies when concentration, improves the effect of purification.
Specific embodiment
It is clearly and completely described below in conjunction with the technical solution in the embodiment of the present invention, it is clear that described reality
Applying example is only a part of the embodiment of the present invention, instead of all the embodiments.Based on the embodiments of the present invention, this field is general
Logical technical staff every other embodiment obtained without making creative work belongs to what the present invention protected
Range.
The embodiment of the present invention provide three kinds of technical solutions: one kind do not purify under the conditions of middle less salt nitre than brine concentration side
Method specifically includes following embodiment:
Embodiment 1
Less salt nitre is screened than brine, centering less salt nitre than brine in S1, acquirement, is repeatedly sieved using screening machine
Choosing, screens out middle less salt nitre than the impurity in brine, obtains the middle less salt nitre without sundries and compares brine；
S2, the component that the middle less salt nitre after screening is obtained to 75KG than brine, and be poured into high-temperature evaporator, to halogen
Water is stirred, and high-temperature evaporator is powered, and is heated to the brine in high-temperature evaporator；
S3, it is stirred in limewash of the middle less salt nitre than 5KG is added in brine, and to the brine after addition limewash,
Mixing time is 15 minutes, and the temperature heated at this time is 10 °, makes the magnesium ion in the calcium hydroxide and brine in limewash
(Mg2) it reacts, generates magnesium hydrate precipitate, remove the magnesium ion (Mg2) in brine, excessive calcium hydroxide (Ca (0H) at this time
2) by sodium sulphate (Na2S04) causticization in brine at sodium hydroxide (NaOH)；
S4, in removing the brine after magnesium ion (Mg), be passed through flue gas, and be stirred, mixing time be 15 minutes,
Make carbon dioxide (CO2) and the sodium hydroxide after causticization in brine in flue gas react generate sodium carbonate, sodium carbonate again with halogen
Calcium ion (Ca) reaction in water generates calcium carbonate (CaCO3) precipitating, removes the calcium ion (Ca2) contained in brine；
S5, sodium hydroxide solution 20 is added, the temperature of high-temperature evaporator is adjusted to 80 DEG C, flocculant is added at the same time
10KG, it is lasting to stir, it is stood using 25 DEG C of temperature, obtaining upper layer is clear halogen, the suspension that bottom is calcium and magnesium deposit；
S6, clear halogen is extracted, calcium-magnesium-containing sediment turbid liquid is taken out there are mud discharge port is taken out in high-temperature evaporator bottom
Enter slurry tank, sediment squeezing is regarded into fertilizer application at cake；
S7, clear halogen is slowly evaporated using high-temperature evaporator, evaporation time is 1 hour, and evaporating temperature is 35 DEG C, is obtained dense
Brine after contracting.
Embodiment 2
Less salt nitre is screened than brine, centering less salt nitre than brine in S1, acquirement, is repeatedly sieved using screening machine
Choosing, screens out middle less salt nitre than the impurity in brine, obtains the middle less salt nitre without sundries and compares brine；
S2, the component that the middle less salt nitre after screening is obtained to 85KG than brine, and be poured into high-temperature evaporator, to halogen
Water is stirred, and high-temperature evaporator is powered, and is heated to the brine in high-temperature evaporator；
S3, it is stirred in limewash of the middle less salt nitre than 10KG is added in brine, and to the brine after addition limewash,
Mixing time is 20 minutes, and the temperature heated at this time is 15 °, makes the magnesium ion in the calcium hydroxide and brine in limewash
(Mg2) it reacts, generates magnesium hydrate precipitate, remove the magnesium ion (Mg2) in brine, excessive calcium hydroxide (Ca (0H) at this time
2) by sodium sulphate (Na2S04) causticization in brine at sodium hydroxide (NaOH)；
S4, in removing the brine after magnesium ion (Mg), be passed through flue gas, and be stirred, mixing time be 25 minutes,
Make carbon dioxide (CO2) and the sodium hydroxide after causticization in brine in flue gas react generate sodium carbonate, sodium carbonate again with halogen
Calcium ion (Ca) reaction in water generates calcium carbonate (CaCO3) precipitating, removes the calcium ion (Ca2) contained in brine；
S5, sodium hydroxide solution 25KG is added, the temperature of high-temperature evaporator is adjusted to 80 DEG C, flocculation is added at the same time
Agent 13KG, it is lasting to stir, it is stood using 30 DEG C of temperature, obtains that upper layer is clear halogen, bottom is the suspended of calcium and magnesium deposit
Liquid；
S6, clear halogen is extracted, calcium-magnesium-containing sediment turbid liquid is taken out there are mud discharge port is taken out in high-temperature evaporator bottom
Enter slurry tank, sediment squeezing is regarded into fertilizer application at cake；
S7, clear halogen is slowly evaporated using high-temperature evaporator, evaporation time is 1.5 hours, and evaporating temperature is 45 DEG C, is obtained
Brine after concentration.
Embodiment 3
Less salt nitre is screened than brine, centering less salt nitre than brine in S1, acquirement, is repeatedly sieved using screening machine
Choosing, screens out middle less salt nitre than the impurity in brine, obtains the middle less salt nitre without sundries and compares brine；
S2, the component that the middle less salt nitre after screening is obtained to 100KG than brine, and be poured into high-temperature evaporator, it is right
Brine is stirred, and high-temperature evaporator is powered, and is heated to the brine in high-temperature evaporator；
S3, it is stirred in limewash of the middle less salt nitre than 15KG is added in brine, and to the brine after addition limewash,
Mixing time is 30 minutes, and the temperature heated at this time is 20 °, makes the magnesium ion in the calcium hydroxide and brine in limewash
(Mg2) it reacts, generates magnesium hydrate precipitate, remove the magnesium ion (Mg2) in brine, excessive calcium hydroxide (Ca (0H) at this time
2) by sodium sulphate (Na2S04) causticization in brine at sodium hydroxide (NaOH)；
S4, in removing the brine after magnesium ion (Mg), be passed through flue gas, and be stirred, mixing time be 30 minutes,
Make carbon dioxide (CO2) and the sodium hydroxide after causticization in brine in flue gas react generate sodium carbonate, sodium carbonate again with halogen
Calcium ion (Ca) reaction in water generates calcium carbonate (CaCO3) precipitating, removes the calcium ion (Ca2) contained in brine；
S5, sodium hydroxide solution 35KG is added, the temperature of high-temperature evaporator is adjusted to 80 DEG C, flocculation is added at the same time
Agent 15KG, it is lasting to stir, it is stood using 35 DEG C of temperature, obtains that upper layer is clear halogen, bottom is the suspended of calcium and magnesium deposit
Liquid；
S6, clear halogen is extracted, calcium-magnesium-containing sediment turbid liquid is taken out there are mud discharge port is taken out in high-temperature evaporator bottom
Enter slurry tank, sediment squeezing is regarded into fertilizer application at cake；
S7, clear halogen is slowly evaporated using high-temperature evaporator, evaporation time is 2 hours, and evaporating temperature is 55 DEG C, is obtained dense
Brine after contracting.
It should be noted that, in this document, relational terms such as first and second and the like are used merely to a reality
Body or operation are distinguished with another entity or operation, are deposited without necessarily requiring or implying between these entities or operation
In any actual relationship or order or sequence.Moreover, the terms "include", "comprise" or its any other variant are intended to
Non-exclusive inclusion, so that the process, method, article or equipment including a series of elements is not only wanted including those
Element, but also including other elements that are not explicitly listed, or further include for this process, method, article or equipment
Intrinsic element.
It although an embodiment of the present invention has been shown and described, for the ordinary skill in the art, can be with
A variety of variations, modification, replacement can be carried out to these embodiments without departing from the principles and spirit of the present invention by understanding
And modification, the scope of the present invention is defined by the appended.
Claims (6)
1. the middle less salt nitre under the conditions of one kind does not purify compares brine concentration method, it is characterised in that: specifically includes the following steps:
Less salt nitre is screened than brine, centering less salt nitre than brine in S1, acquirement, is repeatedly screened using screening machine, sieve
Except middle less salt nitre is than the impurity in brine, obtains the middle less salt nitre without sundries and compare brine；
S2, the component that the middle less salt nitre after screening is obtained to 75KG -100KG than brine, and be poured into high-temperature evaporator,
Brine is stirred, high-temperature evaporator is powered, the brine in high-temperature evaporator is heated；
S3, it is stirred in limewash of the middle less salt nitre than 5KG -15KG is added in brine, and to the brine after addition limewash
It mixes, mixing time is 15-30 minutes, and the temperature heated at this time is 10 °-20 °, is made in the calcium hydroxide and brine in limewash
Magnesium ion (Mg2) reaction, generate magnesium hydrate precipitate, at this time remove brine in magnesium ion (Mg2), excessive calcium hydroxide
(Ca (0H) 2) is by sodium sulphate (Na2S04) causticization in brine at sodium hydroxide (NaOH)；
S4, in removing the brine after magnesium ion (Mg), be passed through flue gas, and be stirred, mixing time be 15-30 minutes,
Make carbon dioxide (CO2) and the sodium hydroxide after causticization in brine in flue gas react generate sodium carbonate, sodium carbonate again with halogen
Calcium ion (Ca) reaction in water generates calcium carbonate (CaCO3) precipitating, removes the calcium ion (Ca2) contained in brine；
S5,20-35KG of sodium hydroxide solution is added, the temperature of high-temperature evaporator is adjusted to 80 DEG C, flocculation is added at the same time
10-15KG of agent, it is lasting to stir, it is stood using 25-35 DEG C of temperature, obtains that upper layer is clear halogen, bottom is calcium and magnesium deposition
The suspension of object；
S6, clear halogen is extracted, high-temperature evaporator bottom is pumped into mud there are mud discharge port is taken out, by calcium-magnesium-containing sediment turbid liquid
Tank is starched, sediment squeezing is regarded into fertilizer application at cake；
S7, clear halogen is slowly evaporated using high-temperature evaporator, evaporation time is 1-2 hours, and evaporating temperature is 35-55 DEG C, is obtained
Brine after to concentration.
2. the middle less salt nitre under the conditions of one kind according to claim 1 does not purify compares brine concentration method, it is characterised in that:
It is emulsified lime slurry that limewash is added in the brine, and the content of active calcium oxide (Ca0) is in the lime slurry
140-220t, relative density are 1.2 to 1.4g/cm, and the additional amount of lime slurry controls the sodium hydroxide (Na0H) in brine
Concentration is 0.05 to 0.3g/L.
3. the middle less salt nitre under the conditions of one kind according to claim 1 does not purify compares brine concentration method, it is characterised in that:
The lime slurry is in lime plus water forms, and the water being added in lime slurry preparation is fresh water or brine.
4. the middle less salt nitre under the conditions of one kind according to claim 1 does not purify compares brine concentration method, it is characterised in that:
The flocculant added in the step S3 is cationic-type polyacrylamide, and additive amount is 1 to 5ppm.
5. the middle less salt nitre under the conditions of one kind according to claim 1 does not purify compares brine concentration method, it is characterised in that:
The flue gas being passed through in the brine is the flue gas generated in boiler using fuel such as heavy oil, natural gas, coals, normal in room temperature
Pressure is slowly introducing in brine, and the carbon dioxide in flue gas is made to react the excessive sodium hydroxide generated with the brine in S4
Reaction generates sodium carbonate, and the intake of flue gas controls between the PH=9 to 12.5 of brine, and the excess of sodium carbonate generated is dense
Degree is 0.1 to 0.8g/L.
6. the middle less salt nitre under the conditions of one kind according to claim 1 does not purify compares brine concentration method, it is characterised in that:
The flue gas is the clean flue gas by purified treatment, and purification process includes: washing, cooling and compression.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112624170A (en) * | 2020-12-08 | 2021-04-09 | 昆明理工大学 | Method for preparing spherical calcite type calcium carbonate from high-calcium sodium sulfate type brine |
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| CN106986356A (en) * | 2017-05-12 | 2017-07-28 | 江西晶昊盐化有限公司 | A kind of lime-flue gas bittern purifying method |
| CN107540072A (en) * | 2017-09-18 | 2018-01-05 | 湖南省湘衡盐化有限责任公司 | A kind of flocculant solution preparation method and bittern purifying method |
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2018
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| US4188291A (en) * | 1978-04-06 | 1980-02-12 | Anderson Donald R | Treatment of industrial waste water |
| CN101289200A (en) * | 2007-04-16 | 2008-10-22 | 中国盐业总公司 | Technological process for purifying bittern |
| CN104909390A (en) * | 2015-05-25 | 2015-09-16 | 江苏久吾高科技股份有限公司 | Membrane-method coupling lime flue gas brine purification process |
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| CN112624170A (en) * | 2020-12-08 | 2021-04-09 | 昆明理工大学 | Method for preparing spherical calcite type calcium carbonate from high-calcium sodium sulfate type brine |
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