CN105254084A - 一种脱硫废水的双极膜电渗析处理方法及装置 - Google Patents
一种脱硫废水的双极膜电渗析处理方法及装置 Download PDFInfo
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- CN105254084A CN105254084A CN201510779923.6A CN201510779923A CN105254084A CN 105254084 A CN105254084 A CN 105254084A CN 201510779923 A CN201510779923 A CN 201510779923A CN 105254084 A CN105254084 A CN 105254084A
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- order reaction
- nanofiltration
- bipolar membrane
- membrane electrodialysis
- desulfurization wastewater
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- 239000002351 wastewater Substances 0.000 title claims abstract description 67
- 230000003009 desulfurizing Effects 0.000 title claims abstract description 59
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 58
- 238000000909 electrodialysis Methods 0.000 title claims abstract description 47
- 239000012528 membrane Substances 0.000 title claims abstract description 38
- 238000006243 chemical reaction Methods 0.000 claims abstract description 93
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- AXCZMVOFGPJBDE-UHFFFAOYSA-L Calcium hydroxide Chemical compound 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[OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims abstract description 10
- 239000000920 calcium hydroxide Substances 0.000 claims abstract description 10
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims abstract description 10
- 238000000034 method Methods 0.000 claims description 49
- 239000006228 supernatant Substances 0.000 claims description 18
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 13
- 239000003795 chemical substances by application Substances 0.000 claims description 13
- 239000003546 flue gas Substances 0.000 claims description 13
- 238000000746 purification Methods 0.000 claims description 11
- 241001274216 Naso Species 0.000 claims description 6
- 238000007792 addition Methods 0.000 claims description 5
- QAOWNCQODCNURD-UHFFFAOYSA-L sulfate Chemical compound 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[O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 4
- 238000005429 turbidity Methods 0.000 claims description 4
- 230000035484 reaction time Effects 0.000 claims description 2
- PMZURENOXWZQFD-UHFFFAOYSA-L na2so4 Chemical compound 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[Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 abstract description 7
- 229910052938 sodium sulfate Inorganic materials 0.000 abstract description 7
- 235000011152 sodium sulphate Nutrition 0.000 abstract description 7
- 239000011575 calcium Substances 0.000 abstract description 6
- 239000002699 waste material Substances 0.000 abstract description 4
- 229910052791 calcium Inorganic materials 0.000 abstract description 3
- 239000011777 magnesium Substances 0.000 abstract description 3
- 239000000203 mixture Substances 0.000 abstract description 3
- 238000000926 separation method Methods 0.000 abstract description 3
- OYPRJOBELJOOCE-UHFFFAOYSA-N calcium Chemical compound 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[Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 abstract description 2
- 229910052749 magnesium Inorganic materials 0.000 abstract description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N magnesium Chemical compound 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[Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 abstract 1
- 239000000463 material Substances 0.000 abstract 1
- 238000002425 crystallisation Methods 0.000 description 8
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- 238000002203 pretreatment Methods 0.000 description 8
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- 238000002360 preparation method Methods 0.000 description 4
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Chemical compound 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Abstract
本发明公开了一种脱硫废水双极膜电渗析处理方法及其装置,包括如下步骤:1)对脱硫废水进行一、二和三级反应处理,分离得到上清液;2)对上清液依次进行超滤和纳滤,得到纳滤浓水和纳滤通过液,所述纳滤浓水投加至二级反应处理中;3)对纳滤通过液进行双极膜电渗析,得到氢氧化钠和盐酸,所述氢氧化钠部分循环至一级反应处理。该装置包括依次连接的一级、二级和三级反应池、超滤装置、纳滤装置和双极膜电渗析装置,所述纳滤装置和所述二级反应池相连通,所述双极膜电渗析装置和所述一级反应池相连通。采用额外投加氢氧化钙、利用自身产生的氢氧化钠和硫酸钠,对钙镁进行去除,使后续物质成分简单,回收容易,不浪费资源,也不污染环境。
Description
技术领域
[0001] 本发明属于脱硫废水处理领域,具体设及一种脱硫废水双极膜电渗析处理方法及 装置。
背景技术
[0002] 目前随着国家排放标准的提高,脱硫废水零排放处理也逐渐开展实施。现有的脱 硫废水工艺一般包括中和、沉淀、混凝、最终中和及泥浆脱水处理等软化预处理(将脱硫废 水加药混凝澄清,去除大部分硬度、碱度W及悬浮物;软化出水进入过滤系统进一步去除悬 浮物;化学反应产生的泥渣进入脱水系统脱泥)、膜浓缩处理(用各种类型的膜,进行浓缩 处理,得到高盐浓缩液)和蒸发浓缩结晶处理,结晶后的浓缩液与晶体颗粒进行固液分离, 母液返回原液池或继续蒸发结晶,晶体进行脱水干燥,最后得到净化水和杂盐。该方案的特 点在于:提高悬浮物、重金属离子、硬度离子、娃离子的去除率,同时将运部分污染物从离子 态蒸发结晶转化为固体态,从废水中分离排放,达到如下效果:一是可W使废水达标排放, 二是可W将废水进行浓缩,Ξ是蒸发结晶后杂盐排放。
[0003] 但是却存在如下缺点:(1)在预处理阶段进行加药软化,碳酸钢投加量很大,运行 成本很高;(2)脱硫废水具有含盐量高、成分复杂、硬度高等特点,同时采用费用较高的传 统蒸发结晶零排放工艺最终产生固体杂盐,杂盐成分复杂无法回收利用,只能作为危废处 理。
[0004] 例如中国专利文献CN202924865U公开了一种脱硫废水膜法处理回收系统,采用 石灰-纯碱软化预处理脱硫废水,再通过纳滤-反渗透除盐,纳滤浓水返回脱硫废水池,反 渗透浓水进蒸发器实现淡水回收和出盐,其使用纳滤的目的是降低反渗透进水中二价结垢 离子浓度,且纳滤浓水返回化学软化预处理继续处理,但其使用了大量化学药剂,成本高。
[0005] 中国专利文献CN103708666A公开了一种脱硫废水回收与零排放处理方法及设 备,该方法依次包括如下步骤:预处理、化学反应处理、分离处理、净化过滤处理和蒸发结晶 处理,首先采用大量化学药剂进行预处理和化学反应处理,然后,又采用了费用较高的传统 蒸发结晶,增加了处理成本,致使得到的固体杂盐成分复杂无法回收利用,只能作为危废处 理,浪费了资源,污染了环境。
[0006] 中国专利文献CN104355473A公开了一种采用电渗析技术进行电厂脱硫废水脱 盐零排放处理的方法,该工艺也采用预处理、电渗析和蒸发浓缩结晶,不但,存在上述种种 问题,而且步骤繁琐,并不能同时得到化0H和HC1。
发明内容
[0007] 本发明的目的在于解决现有技术中对脱硫废水进行预处理时,预处理药剂添加量 大,造成药剂成本过高,化及金属离子(化或Mg等)去除不彻底,造成后续得到固体物质成 分复杂,无法回收利用,浪费资源,污染环境,同时,无法充分利用脱硫废水处理过程中的产 物,达到资源和经济的双重考量的问题,进而提供了一种脱硫废水电渗析处理方法及装置。
[000引为此,本发明采用的技术方案为,
[0009] -种脱硫废水的双极膜电渗析处理方法,包括如下步骤:
[0010] 1)对脱硫废水进行Ξ级反应处理:将脱硫废水和含有氨氧化钢的投加剂混合进 行一级反应处理,分离得到上清液I;再将上清液I、氨氧化巧和含有化s〇4的纳滤浓水投加 剂混合进行二级反应处理,分离得到上清液II;最后,向上清液II中通入电厂净化后的烟 气,进行Ξ级反应处理,分离得到上清液III;
[0011] 2)将步骤1)中的上清液III进行超滤,得到超滤通过液,再对所述超滤通过液进 行纳滤,得到含有化S〇4的纳滤浓水投加剂和纳滤通过液,所述含有化SO4的纳滤浓水投加 剂投加至步骤1)的二级反应处理中;
[0012] 3)对步骤2)中的纳滤通过液进行双极膜电渗析,得到氨氧化钢和盐酸,所述氨氧 化钢部分循环至步骤1)中的一级反应处理中。
[0013] 上述制备方法中,步骤1)中,所述脱硫废水主要是锅炉烟气湿法脱硫(石灰石/ 石膏法)过程中吸收塔的排放水。
[0014] 所述氨氧化钢的添加量使所述脱硫废水的抑> 10. 5,去除水中的大部分重金属 及儀离子,所述脱硫废水的双极膜电渗析处理方法在刚开始,只需投加一次含有氨氧化钢 的投加剂,W后,所需氨氧化钢来自后续产生的氨氧化钢。
[0015] 所述一级反应处理的反应溫度10-50°C,反应时间为0. 5~比。
[0016] 所述氨氧化巧的添加量使所述上清液II中硫酸根离子浓度降至1500-2600mg/l, 具体可为 1900-2600mg/L。
[0017] 所述二级反应处理的反应溫度10-50°C。
[001引所述电厂净化后的烟气中0)2的体积含量为8~15%,所述电厂净化后的烟气是 将烟道气通过烟道气压缩机压缩并经过烟道气洗涂器洗涂过滤后得到。
[0019] 上述制备方法中,步骤2)中,所述超滤通过液的污染指数SDK5。
[0020] 所述纳滤通过液的浊度<1. 0NTU,朗格利尔指数LSK0。
[0021] 上述制备方法中,步骤1)和2)中,所述纳滤浓水为含有硫酸钢的纳滤浓水。
[0022] 上述制备方法中,步骤3)中,所述双极膜电渗析中液体流速控制在5-lOcm/s,溫 度小于45°C。
[0023] 进一步地,一种实现所述脱硫废水电渗析处理方法的装置,包括依次连接的一级 反应池、二级反应池、Ξ级反应池、超滤装置、纳滤装置和双极膜电渗析装置,所述纳滤装置 和所述二级反应池相连通,所述双极膜电渗析装置和所述一级反应池相连通。
[0024] 上述装置中,所述二级反应池上设置有氨氧化巧的加料口。
[0025] 所述Ξ级反应池上设置有(¾的通气口。
[0026]与现有技术相比,本发明具有如下有益效果:
[0027] 1)本发明提供的脱硫废水的双极膜电渗析处理方法,避免了采用传统化学软化预 处理采用石灰加碳酸钢形式,药剂费用较高的问题,有效脱除了脱硫废水中的巧儀离子,本 发明只采用额外投加氨氧化巧、利用处理方法中产生的氨氧化钢和硫酸钢,对脱硫废水中 的主要的巧儀进行去除,使后续物质成分简单,回收容易,即不浪费资源,也不污染环境,达 到资源和经济的双重考量;
[0028] 2)本发明提供的脱硫废水的双极膜电渗析处理方法,通过一级反应处理去除所述 脱硫废水中的儀离子及部分重金属;二级反应处理通过氨氧化巧和纳滤浓水中硫酸钢的反 应来生成石膏,进一步脱去硫酸根离子;再者,在Ξ级反应处理中通入电厂净化后的烟气, 进一步对硬度进行去除,能够对高含盐废水中的巧有效的去除,通过去除巧离子和儀离子, 防止后续工艺中结垢出现,避免了超滤和纳滤处理工艺中膜的堵塞;
[0029] 3)本发明提供的脱硫废水的双极膜电渗析处理方法,通过超滤和纳滤两种工艺的 结合,去除高价离子,进一步分离废水中的一价和二价离子,分离出的硫酸钢,回用到二级 反应池中,降低了药剂费用;
[0030] 4)本发明提供的脱硫废水的双极膜电渗析处理方法,通过双极膜电渗析,分别得 到氨氧化钢和盐酸溶液,其中部分氨氧化钢可W回用到一级反应池中参与沉淀反应,部分 盐酸可W调节系统中膜系统进水的抑,剩余的氨氧化钢和盐酸作为产品可W回收利用,无 废水外排,变废为宝,实现了脱硫废水的零排放,同时避免了蒸发结晶法对于废水处理费用 较高,电费较贵的问题,节约了废水处理成本。
附图说明
[0031] 图1为实施例1中脱硫废水双极膜电渗析处理方法的工艺流程图。
具体实施方式
[0032] 下述各个实施例中的所用的脱硫废水主要是锅炉烟气湿法脱硫(石灰石/石膏 法)过程中吸收塔的排放水,所述脱硫废水的水质指标如下表1所示:
[0033] 表1、脱硫废水水质相关指标
[0034]
[0035]
[003引实施例1、脱硫废水电渗析处理方法: ' ' '
[0037] 按照图1中的工艺流程图进行脱硫废水双极膜电渗析处理,具体步骤如下:
[0038] 1)对脱硫废水进行Ξ级反应处理:将脱硫废水输送至一级反应池,并向所述一级 反应池内投加含有氨氧化钢投加剂(即氨氧化钢水溶液,来自后续步骤,预先来自外界的 投加,待工艺稳定后,无需外界的投加)至所述一级反应池内废水的抑值为11,于20°C下 反应比,去除所述脱硫废水中的儀离子及部分重金属,使儀离子含量低于20mg/L;
[0039] 2)将一级反应池反应完成后的上清液输送至二级反应池(其中包含来自后续的 含有硫酸钢的纳滤浓水),并向二级反应池中投加化(0H) 2,于50°C下,使二级反应池内硫酸 根离子浓度降至2600mg/L;
[0040] 3)将二级反应池反应完成后的上清液输送至Ξ级反应池,并向Ξ级反应池中通入 电厂净化后的烟气(C〇2体积含量为10% ),W进一步降低二级反应池内废水的硬度,其中, 该电厂净化后的烟气可通过将烟道气通过烟道气压缩机压缩并经过烟道气洗涂器洗涂过 滤后得到;
[0041] 4)将Ξ级反应池反应完成后的上清液输送至超滤装置,进行超滤,通过超滤,使超 滤通过液的污染指数SDI为3 ;
[0042] 5)经超滤处理后的超滤通过液输送至纳滤装置,进行纳滤,得到纳滤浓水和纳滤 通过液,其中,纳滤通过液的浊度为0. 5NTU,朗格利尔指数LSK0。纳滤浓水循环至二级反 应池,参与反应;
[0043] 6)将纳滤通过液输送到双极膜电渗析装置中进行电渗析,控制纳滤通过液的流速 为5cm/s,于40°C下进行电渗析,得到浓度10. 1 %氨氧化钢溶液,浓度为8. 3%盐酸溶液,其 中部分氨氧化钢溶液循环至一级反应池中,参与反应。
[0044]实施例2、脱硫废水双极膜电渗析处理方法:
[0045] 按照图1中的工艺流程图进行脱硫废水双极膜电渗析处理,具体步骤如下:
[0046] 1)对脱硫废水进行Ξ级反应处理:将脱硫废水输送至一级反应池,并向所述一级 反应池内投加含有氨氧化钢投加剂(即氨氧化钢水溶液,来自后续步骤)至所述一级反应 池内废水的抑值为12,于50°C下反应0.化,去除所述脱硫废水中的儀离子及部分重金属, 使儀离子含量低于20mg/L;
[0047] 2)将一级反应池反应完成后的上清液输送至二级反应池(其中包含来自后续的 含有硫酸钢的纳滤浓水),并向二级反应池中投加Ca(0H)2,于20°C下,使二级反应池内硫酸 根离子浓度降至1900mg/L;
[0048] 3)将二级反应池反应完成后的上清液输送至Ξ级反应池,并向Ξ级反应池中通入 电厂净化后的烟气(C〇2体积含量为15%),W进一步降低二级反应池内废水的硬度,其中, 该电厂净化后的烟气可通过将烟道气通过烟道气压缩机压缩并经过烟道气洗涂器洗涂过 滤后得到;
[0049] 4)将Ξ级反应池反应完成后的上清液输送至超滤装置,进行超滤,通过超滤,使超 滤通过液的污染指数SDI为4 ;
[0050] 5)经超滤处理后的超滤通过液输送至纳滤装置,进行纳滤,得到纳滤浓水和纳滤 通过液,其中,纳滤通过液的浊度为0. 8NTU,朗格利尔指数LSK0。纳滤浓水循环至二级反 应池,参与反应;
[0051] 6)将纳滤通过液输送到双极膜电渗析装置中进行电渗析,控制纳滤通过液的流速 为lOcm/s,于30°C下进行电渗析,得到浓度10. 2%氨氧化钢溶液,浓度为8. 5%盐酸溶液, 其中部分氨氧化钢溶液循环至一级反应池中,参与反应。
[0052] 实施例3、一种脱硫废水电渗析处理方法的装置:
[0053] -种脱硫废水电渗析处理方法的装置,包括依次连接的一级反应池、二级反应池、 Ξ级反应池、超滤装置、纳滤装置和双极膜电渗析装置,所述纳滤装置和所述二级反应池相 连通,所述双极膜电渗析装置和所述一级反应池相连通;
[0054] 所述二级反应池上设置有氨氧化巧的加料口;
[0055] 所述Ξ级反应池上设置有(¾的通气口。
[0056] 显然,上述实施例仅仅是为清楚地说明所作的举例,而并非对实施方式的限定。对 于所属领域的普通技术人员来说,在上述说明的基础上还可W做出其它不同形式的变化或 变动。运里无需也无法对所有的实施方式予W穷举。而由此所引伸出的显而易见的变化或 变动仍处于本发明创造的保护范围之中。
Claims (8)
1. 一种脱硫废水双极膜电渗析处理方法,包括如下步骤: 1) 对脱硫废水进行三级反应处理:将脱硫废水和含有氢氧化钠的投加剂混合进行一 级反应处理,分离得到上清液I;再将上清液I、氢氧化钙和含有NaS04的纳滤浓水投加剂混 合进行二级反应处理,分离得到上清液II;最后,向上清液II中通入电厂净化后的烟气,进 行三级反应处理,分离得到上清液III; 2) 将步骤1)中的上清液III进行超滤,得到超滤通过液,再对所述超滤通过液进行纳 滤,得到含有NaS04的纳滤浓水投加剂和纳滤通过液,所述含有NaSO4的纳滤浓水投加剂投 加至步骤1)的二级反应处理中; 3) 对步骤2)中的纳滤通过液进行双极膜电渗析,得到氢氧化钠和盐酸,所述氢氧化钠 部分循环至步骤1)中的一级反应处理中。
2. 如权利要求1所述的脱硫废水双极膜电渗析处理方法,其特征在于:步骤1)中,所 述氢氧化钠的添加量使所述脱硫废水的pH> 10. 5 ; 所述一级反应处理的反应温度10_50°C,反应时间为0. 5~lh。
3. 如权利要求1或2所述的脱硫废水双极膜电渗析处理方法,其特征在于:步骤1)中, 所述氢氧化钙的添加量使所述上清液II中硫酸根离子浓度降至1500_2600mg/L; 所述二级反应处理的反应温度10_50°C。
4. 如权利要求1-3中任一项所述的脱硫废水双极膜电渗析处理方法,其特征在于:所 述电厂净化后的烟气中C02的体积含量为8~15%。
5. 如权利要求1-4中任一项所述的脱硫废水双极膜电渗析处理方法,其特征在于:步 骤2)中,所述超滤通过液的污染指数SDK5; 所述纳滤通过液的浊度〈1. 0NTU,朗格利尔指数LSK0。
6. 如权利要求1-5中任一项所述的脱硫废水双极膜电渗析处理方法,其特征在于:步 骤3)中,所述双极膜电渗析中,液体流速为5-lOcm/s,温度< 45°C。
7. 实现权利要求1-6中任一项所述的脱硫废水双极膜电渗析处理方法的装置,包括依 次连接的一级反应池、二级反应池、三级反应池、超滤装置、纳滤装置和双极膜电渗析装置, 所述纳滤装置和所述二级反应池相连通,所述双极膜电渗析装置和所述一级反应池相连 通。
8. 如权利要求7所述的装置,其特征在于:所述二级反应池上设置有氢氧化钙的加料 P; 所述三级反应池上设置有C02的通气口。
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