CN106045113B - 一种制纯碱厂高盐废水的循环利用工艺方法 - Google Patents
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- 238000000034 method Methods 0.000 title claims abstract description 52
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 title claims abstract description 26
- 239000002351 wastewater Substances 0.000 title claims abstract description 21
- 229910000029 sodium carbonate Inorganic materials 0.000 title claims abstract description 10
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 41
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims abstract description 32
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 31
- 229910052925 anhydrite Inorganic materials 0.000 claims abstract description 16
- 239000011780 sodium chloride Substances 0.000 claims abstract description 15
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 15
- 239000012267 brine Substances 0.000 claims abstract description 14
- 230000001376 precipitating effect Effects 0.000 claims abstract description 14
- 239000002253 acid Substances 0.000 claims abstract description 13
- 239000000292 calcium oxide Substances 0.000 claims abstract description 13
- 239000007864 aqueous solution Substances 0.000 claims abstract description 12
- 239000002994 raw material Substances 0.000 claims abstract description 12
- 239000000243 solution Substances 0.000 claims abstract description 12
- 238000004821 distillation Methods 0.000 claims abstract description 11
- 230000018044 dehydration Effects 0.000 claims abstract description 8
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 8
- 238000010521 absorption reaction Methods 0.000 claims abstract description 6
- 238000000926 separation method Methods 0.000 claims abstract description 6
- 230000002328 demineralizing effect Effects 0.000 claims abstract description 3
- 238000004519 manufacturing process Methods 0.000 claims description 7
- 239000001110 calcium chloride Substances 0.000 claims description 6
- 229910001628 calcium chloride Inorganic materials 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 6
- 230000003197 catalytic effect Effects 0.000 claims description 4
- 238000001035 drying Methods 0.000 claims description 4
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 claims description 3
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 3
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 3
- 239000004571 lime Substances 0.000 claims description 3
- 239000007788 liquid Substances 0.000 claims description 3
- 239000002244 precipitate Substances 0.000 claims description 3
- 239000006227 byproduct Substances 0.000 claims description 2
- 238000000354 decomposition reaction Methods 0.000 claims description 2
- 239000000839 emulsion Substances 0.000 claims description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims 1
- 239000005864 Sulphur Substances 0.000 claims 1
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 abstract description 20
- 235000012255 calcium oxide Nutrition 0.000 abstract description 10
- 239000012528 membrane Substances 0.000 abstract description 2
- 238000005119 centrifugation Methods 0.000 abstract 2
- 239000002893 slag Substances 0.000 abstract 2
- -1 containing NaCl Chemical compound 0.000 abstract 1
- 230000005484 gravity Effects 0.000 abstract 1
- 150000003839 salts Chemical class 0.000 description 7
- 235000017550 sodium carbonate Nutrition 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 4
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 238000012545 processing Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
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Classifications
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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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- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
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- C01B17/745—Preparation from sulfates
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- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
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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
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Abstract
本发明涉及一种制纯碱厂高盐废水的循环利用工艺方法,该方法包括如下步骤:(1)按废水中CaCl2和硫酸摩尔浓度1:1的量,向废水中加入浓硫酸,生成CaSO4沉淀和盐酸,CaSO4沉淀在重力作用下沉积在反应器底部,并排入沉淀储池,上部水溶液则进入耐酸储水池;(2)储存在沉淀储池中的CaSO4沉淀通过离心分离进一步脱水,离心后的饼渣储存备用,离心后的水溶液进入耐酸储水池;(3)以CaSO4饼渣为原料,通过焙烧法再制取浓硫酸,同时获得生石灰CaO,浓硫酸回用至步骤(1),实现浓硫酸的闭路循环;(4)耐酸储水池中的酸溶液通过蒸馏或膜吸收法去除盐酸,得到主要含NaCl的浓盐水,NaCl浓盐水将作为原料回用到制碱工艺过程中。
Description
技术领域
本发明涉及一种制纯碱厂高盐废水的循环利用工艺方法,属于资源综合利用技术领域。
背景技术
化工行业生产纯碱的工艺中,需要消耗大量的淡水资源并产生大量的高浓度含盐废水,在水资源匮乏的西部地区,产生的大量高浓度含盐废水如果得不到妥善处理和处置,不仅造成严重的环境污染问题,更是造成水资源的严重浪费,严重制约了相关企业的发展。为此,在这些地区,高浓度含盐废水的再生和资源化将是首要选择。
目前含盐废水的处理技术主要有离子交换、反渗透、电渗析、蒸馏等方法,通过这些方法可以实现含盐废水的浓缩和减量。而在实际的工艺过程中,往往不是简单的脱盐过程,而是需要选择性脱出某一个或某一类盐,并回收利用其中某一个或某一类盐。这就需要根据实际工艺过程需要,从循环经济和绿色化学的角度出发,创新提出高盐废水的处理处置方案。
发明内容
针对纯碱生产工艺过程排放的高浓度含盐废水(CaCl2、NaCl为主要盐类),其中CaCl2约120g/L,NaCl约50g/L,NaCl为制纯碱过程的原料,CaCl2为需要去除的盐类。由此从物料循环和资源再利用的角度出发,本发明提供了一种一种制纯碱厂高盐废水的循环利用工艺方法。
一种制纯碱厂高盐废水的循环利用工艺方法,包括如下步骤:
(1)加酸沉淀:向废水中直接添加浓硫酸,生成CaSO4沉淀和盐酸,经过固液分离,CaSO4沉淀排入沉淀储池,水溶液则进入耐酸储水池。本步骤涉及的反应如下:
CaCl2+H2SO4→CaSO4↓+2HCl
(2)沉淀脱水:沉淀储池中的CaSO4经过脱水、干燥后作为后续浓硫酸循环生产的原料,脱水水溶液排入耐酸储水池;
(3)浓硫酸循环:以离心干燥后硫酸钙(CaSO4)为原料,采用焙烧法制取浓硫酸,浓硫酸回用至步骤(1),同时产生石灰CaO。具体方法有两种,一是CaSO4在高温下煅烧,温度高于1200℃,直接分解为CaO、SO2和O2,SO2和O2进入催化塔被氧化为SO3,SO3在吸收塔中被硫酸水溶液吸收得到浓硫酸,涉及反应如下:
2CaSO4→2CaO+2SO2↑+O2↑
2SO2+O2→2SO3
SO3+H2O→H2SO4
二是在碳粉参与下,CaSO4在高温下焙烧,分解为CaO和SO2,SO2在催化塔中被氧化为SO3,并在吸收塔中被硫酸水溶液吸收,最后得到浓硫酸,涉及反应如下:
2CaSO4+C→2CaO+2SO2↑+CO2↑
2SO2+O2→2SO3
SO3+H2O→H2SO4
(4)盐酸分离:耐酸储水池中的水溶液主要含NaCl和盐酸,将盐酸分离后,NaCl水溶液将作为原料回用至制纯碱生产工艺过程中。盐酸分离的方法优选两种,一是通过蒸馏法去除水溶液中的盐酸,浓缩后的NaCl浓盐水回用至制纯碱工艺中;二是通过膜吸收法去除水溶液中的盐酸,得到的NaCl盐水回用至制纯碱工艺中。
本发明通过物料的内循环设计,使整个高盐废水的分离再生过程不需外加任何物料,同时只产生生石灰CaO及有价值的盐酸,整个工艺过程绿色、环保,基本实现零排放。
附图说明
图1是本发明所述方法的示意图。
具体实施方式
下面结合附图对本发明的实施例进行详细说明。
实施例1
一种制纯碱厂高盐废水的循环利用工艺方法,其特征在于,该方法主要包括如下步骤:
步骤一、加酸沉淀:按废水中CaCl2和硫酸摩尔浓度1:1的量,向废水中加入浓硫酸(>90%),生成CaSO4沉淀和HCl,经过固液分离,CaSO4沉淀排入沉淀储池,水溶液则进入耐酸储水池;
步骤二、沉淀脱水:沉淀储池中的CaSO4通过脱水、干燥后储存待用,脱水水溶液排入耐酸储水池;
步骤三、浓硫酸循环:以干燥CaSO4为原料,采用焙烧法制取浓硫酸,浓硫酸回用至步骤一,同时产生石灰CaO,具体方法为CaSO4在高温下焙烧分解为CaO和SO2,SO2在催化塔中被氧化为SO3,并在吸收塔中被硫酸水溶液吸收,最后得到浓硫酸;
步骤四、蒸馏:耐酸储水池中的含盐酸溶液,在蒸馏作用下去除盐酸,得到浓缩后的NaCl浓盐水和蒸馏得到的盐酸溶液,或者在膜吸收的条件下用CaO乳液吸收HCl得到CaCl2溶液和NaCl浓盐水;NaCl浓盐水将作为原料,回用至制纯碱工艺中;在不考虑操作过程物料损失条件下,所述方法不需要外加任何物料,其中,所用的浓硫酸在整个工艺过程中闭路循环。沉淀反应后的含盐酸溶液通过蒸馏或者膜吸收去除HCl,得到含NaCl的浓盐水,该浓盐水将作为原料回用至制碱工艺过程,蒸馏所得到的高纯盐酸溶液或者膜吸收得到的氯化钙为副产物。
Claims (2)
1.一种制纯碱厂高盐废水的循环利用工艺方法,其特征在于,该方法主要包括如下步骤:
步骤一、加酸沉淀:按废水中CaCl2和硫酸摩尔浓度1:1的量,向废水中加入浓硫酸,所述浓硫酸的浓度>90%,生成CaSO4沉淀和HCl,经过固液分离,CaSO4沉淀排入沉淀储池,水溶液则进入耐酸储水池;
步骤二、沉淀脱水:沉淀储池中的CaSO4通过脱水、干燥后储存待用,脱水水溶液排入耐酸储水池;
步骤三、浓硫酸循环:以CaSO4为原料,采用焙烧法制取浓硫酸,浓硫酸回用至步骤一,同时产生石灰CaO,具体方法为CaSO4在高温下焙烧分解为CaO和SO2,SO2在催化塔中被氧化为SO3,并在吸收塔中被硫酸水溶液吸收,最后得到浓硫酸;
步骤四、蒸馏:耐酸储水池中的含盐酸溶液,在蒸馏作用下去除盐酸,得到浓缩后的NaCl浓盐水和蒸馏得到的盐酸溶液,或者在膜吸收的条件下用CaO乳液吸收HCl得到CaCl2溶液和NaCl浓盐水;NaCl浓盐水将作为原料,回用至制纯碱工艺中;
在不考虑操作过程物料损失条件下,所述方法不需要外加任何物料,其中,所用的浓硫酸在整个工艺过程中闭路循环。
2.如权利要求1所述的方法,其特征在于:加酸沉淀和沉淀脱水反应后的含盐酸溶液通过蒸馏或者膜吸收去除HCl,得到含NaCl的浓盐水,该浓盐水将作为原料回用至制碱工艺过程,蒸馏所得到的高纯盐酸溶液或者膜吸收得到的氯化钙为副产物。
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CN101200285A (zh) * | 2007-11-19 | 2008-06-18 | 康仁 | 一种生产聚氯乙烯和盐酸的方法 |
CN101219797A (zh) * | 2008-01-28 | 2008-07-16 | 王晓璐 | 纳滤膜技术分离蒸氨废清液中氯化钙和氯化钠的方法及该方法产物的应用 |
CN101830584A (zh) * | 2010-04-30 | 2010-09-15 | 汪晋强 | 一种用盐酸处理纯碱蒸馏废液形成的方法 |
CN103043627A (zh) * | 2012-12-21 | 2013-04-17 | 刘立文 | 一种用硫酸钙生产硫酸的设备 |
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JPH04293597A (ja) * | 1991-03-20 | 1992-10-19 | Tokio Saitou | 整地固化剤 |
CN101200285A (zh) * | 2007-11-19 | 2008-06-18 | 康仁 | 一种生产聚氯乙烯和盐酸的方法 |
CN101219797A (zh) * | 2008-01-28 | 2008-07-16 | 王晓璐 | 纳滤膜技术分离蒸氨废清液中氯化钙和氯化钠的方法及该方法产物的应用 |
CN101830584A (zh) * | 2010-04-30 | 2010-09-15 | 汪晋强 | 一种用盐酸处理纯碱蒸馏废液形成的方法 |
CN103043627A (zh) * | 2012-12-21 | 2013-04-17 | 刘立文 | 一种用硫酸钙生产硫酸的设备 |
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